EP2415819A2 - Porcess of making sugars from biomass - Google Patents

Porcess of making sugars from biomass Download PDF

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Publication number
EP2415819A2
EP2415819A2 EP11007762A EP11007762A EP2415819A2 EP 2415819 A2 EP2415819 A2 EP 2415819A2 EP 11007762 A EP11007762 A EP 11007762A EP 11007762 A EP11007762 A EP 11007762A EP 2415819 A2 EP2415819 A2 EP 2415819A2
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EP
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Prior art keywords
feedstock
molecular weight
biomass
percent
radiation
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
EP11007762A
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German (de)
French (fr)
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EP2415819A3 (en
Inventor
Marshall Medoff
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Xyleco Inc
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Xyleco Inc
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Application filed by Xyleco Inc filed Critical Xyleco Inc
Publication of EP2415819A2 publication Critical patent/EP2415819A2/en
Publication of EP2415819A3 publication Critical patent/EP2415819A3/en
Ceased legal-status Critical Current

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    • F01K7/16Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating the engines being only of turbine type
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    • F01MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01KSTEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K9/00Plants characterised by condensers arranged or modified to co-operate with the engines
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22STEAM GENERATION
    • F22BMETHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00Methods of steam generation characterised by form of heating method
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    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10Feedstock materials
    • C10G2300/1003Waste materials
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    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10G2300/00Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10Feedstock materials
    • C10G2300/1011Biomass
    • C10G2300/1014Biomass of vegetal origin
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    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10LFUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2200/00Components of fuel compositions
    • C10L2200/04Organic compounds
    • C10L2200/0461Fractions defined by their origin
    • C10L2200/0469Renewables or materials of biological origin
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    • C10L2250/00Structural features of fuel components or fuel compositions, either in solid, liquid or gaseous state
    • C10L2250/04Additive or component is a polymer
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    • C10L2250/00Structural features of fuel components or fuel compositions, either in solid, liquid or gaseous state
    • C10L2250/06Particle, bubble or droplet size
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    • C10L2290/00Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/02Combustion or pyrolysis
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    • C10L2290/00Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/26Composting, fermenting or anaerobic digestion fuel components or materials from which fuels are prepared
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    • C10L2290/00Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/28Cutting, disintegrating, shredding or grinding
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    • C10L2290/00Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/34Applying ultrasonic energy
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    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10LFUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/36Applying radiation such as microwave, IR, UV
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10LFUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/38Applying an electric field or inclusion of electrodes in the apparatus
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10LFUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/48Expanders, e.g. throttles or flash tanks
    • CCHEMISTRY; METALLURGY
    • C12BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12PFERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P2201/00Pretreatment of cellulosic or lignocellulosic material for subsequent enzymatic treatment or hydrolysis
    • CCHEMISTRY; METALLURGY
    • C12BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12PFERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P2203/00Fermentation products obtained from optionally pretreated or hydrolyzed cellulosic or lignocellulosic material as the carbon source
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00Technologies for the production of fuel of non-fossil origin
    • Y02E50/10Biofuels, e.g. bio-diesel
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00Technologies for the production of fuel of non-fossil origin
    • Y02E50/30Fuel from waste, e.g. synthetic alcohol or diesel
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00Technologies relating to oil refining and petrochemical industry
    • Y02P30/20Technologies relating to oil refining and petrochemical industry using bio-feedstock
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P60/00Technologies relating to agriculture, livestock or agroalimentary industries
    • Y02P60/80Food processing, e.g. use of renewable energies or variable speed drives in handling, conveying or stacking
    • Y02P60/87Re-use of by-products of food processing for fodder production
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02WCLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00Technologies for solid waste management
    • Y02W30/50Reuse, recycling or recovery technologies
    • Y02W30/64Paper recycling

Definitions

  • This invention relates to processing biomass, and products made therefrom.
  • Cellulosic and lignocellulosic materials are produced, processed, and used in large quantities in a number of applications. Often such materials are used once, and then discarded as waste, or are simply considered to be waste materials, e.g., sewage, bagasse, sawdust, and stover.
  • the invention features methods of changing a molecular structure of a biomass feedstock that include preparing the biomass feedstock by reducing one or more dimensions of individual pieces of biomass; pretreating the biomass feedstock using two or more different pretreatment methods that each change the molecular structure, in which the different pretreatment methods are selected from radiation, sonication, pyrolysis, and oxidation; and processing the prepared and pretreated biomass feedstock to produce a product.
  • the biomass feedstock is prepared and then pretreated.
  • the biomass feedstock can also be pretreated and then prepared.
  • Reducing one or more dimensions of individual pieces of biomass can include, e.g., shearing, cutting, or grinding.
  • the two or more pretreatment methods are applied to the biomass feedstock at or about the same time.
  • the two or more pretreatment methods can include radiation and sonication.
  • the radiation can be in the form of an electron beam.
  • the electron beam radiation is applied at a total dosage of about 10 MRad and the sonication is applied at a total energy of more than 5 MJ/m 3 .
  • Radiation can precede sonication, or sonication can precede radiation, or radiation and sonication can performed at or about the same time.
  • the change in molecular structure of the biomass feedstock can include a change in any one or more of an average molecular weight, average crystallinity, surface area, polymerization, porosity, branching, grafting, and domain size of the biomass.
  • the change in molecular structure of the biomass feedstock includes a decrease in either one or both of an average molecular weight and average crystallinity of the biomass or an increase in either one or both of surface area and porosity of the biomass.
  • the invention features methods of making products, such as combustible fuels, that include providing a material that includes a carbohydrate produced by a process that includes pretreating a biomass feedstock with any two or more of radiation, sonication, pyrolysis, and oxidation; and contacting the material with a microorganism having the ability to convert at least a portion, e.g., at least about 1 percent by weight, of the material to the product, such as a combustible fuel.
  • the two or more different pretreatment methods include radiation and sonication, radiation and oxidation, radiation and pyrolization, sonication and oxidation, sonication and pyrolization, or oxidation and pyrolization.
  • any method described herein can further include pretreating the biomass feedstock with steam explosion.
  • the process does not include hydrolyzing the biomass with an acid or a base.
  • At least about seventy percent by weight of the biomass is unhydrolyzed, e.g., at least at 95 percent by weight of the biomass has not been hydrolyzed. In specific embodiments, substantially none of the biomass has been hydrolyzed.
  • At least one pretreatment method is performed on biomass in which less than about 25 percent by weight of the biomass is wetted with a liquid, such as water.
  • at least one pretreatment method is performed on biomass in which substantially none of the biomass is wetted with a liquid, such as water.
  • the biomass can have, e.g., less than about five percent by weight retained water, measured at 25°C and at fifty percent relative humidity.
  • At least one pretreatment method can be performed on biomass in which less than about 25 percent by weight of the biomass is in a swollen state, the swollen state being characterized as having a volume of more than about 2.5 percent higher than an unswollen state.
  • the biomass is mixed with or includes a swelling agent.
  • the biomass can be mixed with or and include a swelling agent, and the biomass can receives a dose of less than about 10 Mrad of radiation.
  • one of the pretreatment methods is or includes radiation.
  • At least one of the pretreatment methods is performed on the biomass feedstock while the biomass feedstock is exposed to air.
  • Pressure can be utilized.
  • at least one of the pretreatment methods e.g., radiation
  • the process can further include oxidizing, pyrolizing, or steam exploding the biomass.
  • biomass feedstock examples include paper, paper products, paper waste, wood, particle board, sawdust, agricultural waste, sewage, silage, grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, corn stover, switchgrass, alfalfa, hay, rice hulls, coconut hair, cotton, synthetic celluloses, seaweed, algae, or mixtures of these.
  • the biomass can be or can include a natural or a synthetic material.
  • Examples of fuels include one or more of hydrogen, alcohols, and hydrocarbons:
  • the alcohols can be ethanol, n-propanol, isoproanol, n-butanol, or mixtures of these.
  • the microorganism can be, e.g., a bacterium or a yeast.
  • Converting can include fermenting the material to the product, such as the combustible fuel.
  • Irradiation can be, e.g., performed utilizing an ionizing radiation, such as gamma rays, a beam of electrons, or ultraviolet C radiation having a wavelength of from about 100 nm to about 280 nm.
  • an ionizing radiation such as gamma rays, a beam of electrons, or ultraviolet C radiation having a wavelength of from about 100 nm to about 280 nm.
  • the ionizing radiation can include electron beam radiation.
  • the radiation can be applied at a total dose of between about 10 Mrad and about 150 Mrad, such as at a dose rate of about 0.5 to about 10 Mrad/day, or 1 Mrad/s to about 10 Mrad/s.
  • irradiating includes applying two or more radiation sources, such as gamma rays and a beam of electrons.
  • sonication can be performed at a frequency of between about 15 kHz and about 25 kHz, such as between about 18 kHz and 22 kHz.
  • the biomass includes a first cellulose having a first number average molecular weight and the carbohydrate material comprises a second cellulose having a second number average molecular weight lower than the first number average molecular weight.
  • the second number average molecular weight is lower than the first number average molecular weight by more than about one-fold.
  • the first cellulose has a first crystallinity
  • the second cellulose has a second crystallinity lower than the first crystallinity.
  • the second crystallinity can be lower than the first crystallinity by more than about 10 percent.
  • the first cellulose can have a first level of oxidation and the second cellulose has a second level of oxidation higher than the first level of oxidation.
  • the carbohydrate can include one or more ⁇ -1,4-linkages and having a number average molecular weight between about 3,000 and 50,000.
  • the pretreated biomass material can further include a buffer, such as sodium bicarbonate or ammonium chloride, an electrolyte, such as potassium chloride or sodium chloride a growth factor, such as biotin and/or a base pair such as uracil, a surfactant, a mineral, or a chelating agent.
  • a buffer such as sodium bicarbonate or ammonium chloride
  • an electrolyte such as potassium chloride or sodium chloride
  • a growth factor such as biotin and/or a base pair such as uracil, a surfactant, a mineral, or a chelating agent.
  • the biomass feedstock is pretreated using any three or more of radiation, sonication, pyrolysis, and oxidation, in any order, or at about the same time.
  • the invention features methods of making a product, such as a combustible fuel that include providing a material that includes a carbohydrate produced by pretreating a biomass feedstock with any one or more of radiation, sonication, oxidation, pyrolysis, and steam explosion, wherein less than about 25 percent by weight of the biomass is hydrolyzed subsequent to pretreatment; and contacting the material with a microorganism having the ability to convert at least a portion of the material, e.g., at least about 1 percent by weight, to the product, such as the combustible fuel.
  • the invention features methods of making a product, such as a combustible fuel, that includes providing a material includes a carbohydrate produced by pretreating a biomass feedstock with any one or more of radiation, sonication, oxidation, pyrolysis, and steam explosion, in which less than about 25 percent by weight of the biomass is in contact with a liquid, such as water, and contacting the material with a microorganism having the ability to convert at least a portion, e.g., at least about 1 percent by weight, of the material to the product, such as the combustible fuel.
  • the methods include selecting two or more different pretreatment methods.
  • the two or more different pretreatment methods can include radiation and sonication, radiation and oxidation, radiation and pyrolization, sonication and oxidation, sonication and pyrolization, or oxidation and pyrolization.
  • pretreating the biomass can include steam explosion.
  • the invention features methods of making a product, such as a combustible fuel, that include providing a material comprising a carbohydrate produced by pretreating a sheared biomass feedstock with any one or more of radiation, sonication, oxidation, pyrolysis, and steam explosion; and contacting the material with a microorganism having the ability to convert at least a portion, e.g., at least about 1 percent by weight, of the material to the product, such as the combustible fuel.
  • the sheared biomass can include discrete fibers having a length-to-diameter ratio (L/D) of greater than about 5/1.
  • the biomass can have internal fibers, and the biomass has been sheared to an extent that its internal fibers are substantially exposed.
  • the biomass has been sheared to an extent that it has a bulk density of less than about 0.35 g/cm 3 .
  • the invention features biomass feedstock processing systems tat include a biomass feedstock preparation module for reducing size of pieces of biomass; two or more of the following pretreatment modules: a radiation module arranged to apply radiation to the biomass; a sonication module arranged to apply sonic energy to the biomass; an oxidation module arranged to oxidize the biomass; a pyrolysis module arranged to apply heat to the biomass; and a biomass transportation subsystem to move the biomass to and between modules within the processing system.
  • the two or more pretreatment modules are arranged in series and/or are arranged to treat a portion of the biomass at about the same time.
  • any system can further include a vessel.
  • the invention features systems that include a reaction vessel containing a pretreated biomass material that includes a carbohydrate.
  • the pretreated biomass material is produced by any method described herein.
  • the vessel can also contains a microorganism in contact with the material, the microorganism having the ability to convert at least a portion of the material to a product, such as a combustible fuel.
  • the vessel can have a total volume of greater than about 1,000 L, such as greater than 5,000 L.
  • any system can include a radiation module and a sonication module.
  • the invention features carbohydrate materials produced by a process that includes pretreating a sheared biomass feedstock with any one or more of radiation, sonication, oxidation, pyrolysis and steam explosion.
  • pretreating can be performed with any two or more of radiation, sonication, oxidation, pyrolysis, and steam explosion.
  • the invention features carbohydrate materials produced by a process that includes pretreating a biomass feedstock with any two or more of radiation, sonication, oxidation, pyrolysis, and steam explosion.
  • the invention features compositions that include a cellulosic or a lignocellulosic material having a peak maximum molecular weight of less than about 25,000, and a crystallinity of less than about 55 percent.
  • the cellulosic or a lignocellulosic material can have a porosity of greater than about 72 percent, a BET surface greater than about 0.75 m 2 /g, or a bulk density of less than about 0.5 g/cm 3 .
  • the composition can further include an enzyme and/or a microbe.
  • the invention features compositions that include a cellulosic or a lignocellulosic material that includes fibers.
  • the cellulosic or lignocellulosic material has a peak maximum molecular weight of less than about 25,000, and a bulk density of less than about 0.5 g/cm 3 .
  • the invention features methods of making composites, such as a fiber-resin composite that include irradiating a fibrous material that includes a first cellulosic and/or lignocellulosic material having a first molecular weight to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight; and combining the second cellulosic and/or lignocellulosic material with a material, such as a resin.
  • a material such as a resin
  • the invention features methods of making composites, such as a fiber-resin composite, that include combining a material, such as a resin, with a fibrous material that includes a cellulosic and/or lignocellulosic material having a first molecular weight to provide a composite that includes the fibrous material and a matrix; and irradiating the composite to increase molecular weight of the first cellulosic and/or lignocellulosic material within the matrix, such as a resin matrix.
  • a material such as a resin
  • the invention features methods of making composites, such as a fiber-resin composites that include irradiating a fibrous material that includes a first cellulosic and/or lignocellulosic material having a first molecular weight to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight; combining the second cellulosic and/or lignocellulosic material with a material, such as a resin, to provide a composite; and irradiating the composite.
  • a fibrous material that includes a first cellulosic and/or lignocellulosic material having a first molecular weight to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight
  • a material such as a resin
  • the invention features methods of making irradiated wood products that include providing a wood product that includes a first carbohydrate-containing material having a first molecular weight; and irradiating the wood product to provide an irradiated wood product that includes a second carbohydrate-containing material having a second molecular weight higher than the first molecular weight.
  • the methods can further include sonicating, e.g., prior to, after, or concurrently with the irradiating.
  • the first material includes a cellulosic or a lignocellulosic material.
  • the first material can be or can include paper, paper products, wood, wood-related materials, particle board, grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, rice hulls, algae, seaweed, coconut hair, cotton, synthetic celluloses or mixtures of any of these materials.
  • the first material is in the form of a fibrous material that includes fibers provided by shearing a fiber source.
  • Shearing alone can reduce the crystallinity of a fibrous material and can work synergistically with any process technique that also reduces crystallinity and/or molecular weight.
  • the shearing can be performed with a rotary knife cutter.
  • the fibrous material has an average length-to-diameter ratio of greater than 5/1.
  • the first and/or second material can have, e.g., a BET surface area of greater than 0.25 m 2 /g and/or a porosity of greater than about 25 percent.
  • the irradiating is performed with an ionizing radiation, such as gamma rays or a beam of electrons.
  • an ionizing radiation such as gamma rays or a beam of electrons.
  • the microorganism is a bacterium or a fungus, such as a yeast.
  • the second number average molecular weight is at least about 25 percent lower than the first number average molecular weight, e.g., 50 percent lower.
  • Methods include shearing a fiber source to provide a first fibrous material that includes cellulose having a first number average molecular weight; and irradiating the first fibrous material to provide a second fibrous material that includes a cellulose having a second number average molecular weight lower that the first number average molecular weight.
  • Shearing can work synergistically with radiation to reduce crystallinity and/or molecular weight.
  • Such methods may further include combining the second material with a microorganism.
  • Methods include irradiating a fiber source, e.g., a paper, that includes cellulose having a first number average molecular weight to provide an irradiated fiber source that includes cellulose having a second number average molecular weight less than the first number average molecular weight; and shearing the irradiated fiber source to provide a fibrous material.
  • a fiber source e.g., a paper
  • the irradiated material can be brittle and more susceptible to "opening up" during the shearing.
  • Such methods can further include combining the fibrous material with a microorganism.
  • Methods include providing a first lignocellulosic material that includes cellulose having a first number average molecular weight; and irradiating the first lignocellulosic material to provide a second lignocellulosic material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight.
  • Such methods can further include combining the second lignocellulosic material with a microorganism or removing lignin from the second lignocellulosic material to provide a de-lignified material, and then combining the de-lignified material with a microorganism the microorganism.
  • the lignin from the processing can be utilized as a processing aid for plastics or it can be burned to produce energy.
  • Methods include providing a first fibrous material that includes cellulose having a first number average molecular weight; densifying the first fibrous material to provide a densified first fibrous material; and irradiating the densified first fibrous material to provide a densified second material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight.
  • Densification can work synergistically with irradiation to lower molecular weight and can also increase throughput in any processing step described herein.
  • Such methods can further include combining the second densified fibrous material with a microorganism or fiberizing the second densifed fibrous material to provide a second fibrous material, and then combining the second fibrous material with a microorganism.
  • Methods include sonicating a first material that includes cellulose having a first number average molecular weight to provide a second material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight; and combining the second material with a microorganism.
  • the microorganism utilizes, e.g., ferments or otherwise converts, the second material, and in some instances the first material, to produce a useful material, e.g., a combustible fuel.
  • the combustible fuel can be or can include hydrogen, an alcohol, an organic acid, a hydrocarbon or mixtures of these.
  • a preferred material is ethanol or butanol, e.g., n-, sec- to t-butanol.
  • the first material includes a cellulosic or a lignocellulosic material.
  • the first material can be or can include paper, paper products, wood, wood-related materials, particle board, grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, rice hulls, algae, seaweed, coconut hair, cotton, synthetic celluloses or mixtures of any of these materials.
  • the first material is in the form of a fibrous material that includes fibers provided by shearing a fiber source.
  • Shearing can work synergistically with sonication to reduce molecular weight and/or crystallinity.
  • the shearing can be performed with a rotary knife cutter.
  • the fibrous material has an average length-to-diameter ratio of greater than 5/1.
  • the first and/or second material can have, e.g., a BET surface area of greater than 0.25 m 2 /g and/or a porosity of greater than about 25 percent.
  • the sonicating is performed with sound having a frequency of from about 16 kHz to about 100 kHz and/or an intensity of from about 30 W/cm 2 to about 600 W/cm 2 .
  • the microorganism is a bacterium or a fungus, such as a yeast.
  • the second number average molecular weight is at least about 25 percent lower than the first number average molecular weight, e.g., 50 percent lower.
  • Methods include shearing a fiber source to provide a first fibrous material that includes cellulose having a first number average molecular weight; and sonicating the first fibrous material to provide a second fibrous material that includes a cellulose having a second number average molecular weight lower that the first number average molecular weight.
  • Such methods may further include combining the second material with a microorganism.
  • Methods include sonicating a fiber source, e.g., a paper, that includes cellulose having a first number average molecular weight to provide a sonicated fiber source that includes cellulose having a second number average molecular weight less than the first number average molecular weight; and shearing the sonicated fiber source to provide a fibrous material.
  • a fiber source e.g., a paper
  • the sonicated material can be brittle and more susceptible to "opening up" during the shearing.
  • Such methods can further include combining the fibrous material with a microorganism.
  • Methods include sonicating a first lignocellulosic material that includes cellulose having a first number average molecular weight to provide a second lignocellulosic material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight.
  • Such methods can further include combining the second lignocellulosic material with a microorganism or removing lignin from the second lignocellulosic material to provide a de-lignified material, and then combining the de-lignified material with a microorganism the microorganism.
  • Methods include sonicating a first fibrous material that includes cellulose having a first number average molecular weight to provide a second fibrous material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight; and densifying the second fibrous material to provide a densified fibrous material.
  • Such methods can further include combining the densified fibrous material with a microorganism or fiberizing the densified fibrous material to provide a third fibrous material, and then combining the third fibrous material with a microorganism.
  • an enzyme e.g., a cellulolytic enzyme, or a chemical, e.g., sodium hypochlorite, an acid, a base or a swelling agent, can be utilized with any method described herein.
  • the enzyme and/or chemical treatment can occur before, during or after sonication.
  • Methods include pyrolyzing a first material that includes cellulose having a first number average molecular weight to provide a second material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight; and combining the second material with a microorganism.
  • the microorganism utilizes, e.g., ferments or otherwise converts, the second material, and in some instances the first material, to produce a useful material, e.g., a combustible fuel.
  • the combustible fuel can include one or more of hydrogen, an alcohol, an organic acid, a hydrocarbon or mixtures of these.
  • a preferred material is ethanol or butanol.
  • the first material includes a cellulosic or a lignocellulosic material.
  • the first material can be or can include paper, paper products, wood, wood-related materials, particle board, grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, rice hulls, algae, seaweed, coconut hair, cotton, synthetic celluloses or mixtures of any of these materials.
  • the first material is in the form of a fibrous material that includes fibers provided by shearing a fiber source. Relatively small cross-section can often be pyrolyzed with greater control and efficiency.
  • the shearing can be performed with a rotary knife cutter.
  • the fibrous material has an average length-to-diameter ratio of greater than 5/1.
  • the first and/or second material can have, e.g., a BET surface area of greater than 0.25 m 2 /g and/or a porosity of greater than about 25 percent. High surface areas and/or porosities can enhance reaction rates, making processes more efficient.
  • the microorganism is a bacterium or a fungus, such as a yeast.
  • the second number average molecular weight is at least about 25 percent lower than the first number average molecular weight, e.g., 50 percent lower.
  • Methods include shearing a fiber source to provide a first fibrous material that includes cellulose having a first number average molecular weight; and pyrolyzing the first fibrous material to provide a second fibrous material that includes a cellulose having a second number average molecular weight lower that the first number average molecular weight.
  • Such methods may further include combining the second material with a microorganism.
  • Methods that include pyrolyzing a fiber source, e.g., a paper, that includes cellulose having a first number average molecular weight to provide a pyrolyzed fiber source that includes cellulose having a second number average molecular weight less than the first number average molecular weight; and shearing the pyrolyzed fiber source to provide a fibrous material.
  • a fiber source e.g., a paper
  • the pyrolyzed material can be brittle and more susceptible to "opening up" during the shearing.
  • Shearing pyrolyzed material can be less energy intensive and can be more efficient.
  • Such methods can further include combining the fibrous material with a microorganism.
  • Methods include pyrolyzing a first lignocellulosic material that includes cellulose having a first number average molecular weight to provide a second lignocellulosic material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight.
  • Such methods can further include combining the second lignocellulosic material with a microorganism or removing lignin from the second lignocellulosic material to provide a de-lignified material, and then combining the de-lignified material with a microorganism the microorganism.
  • Methods include pyrolyzing a first fibrous material that includes cellulose having a first number average molecular weight to provide a second fibrous material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight; and densifying the second fibrous material to provide a densified fibrous material.
  • Such methods can further include combining the densified fibrous material with a microorganism or fiberizing the densified fibrous material to provide a third fibrous material, and then combining the third fibrous material with a microorganism.
  • an enzyme e.g., a cellulolytic enzyme, or a chemical, e.g., sodium hypochlorite or an acid or base, can be utilized with any method described herein.
  • the enzyme and/or chemical treatment can occur before, during or after pyrolyzing.
  • pyrolyzing may include any one or more of the following features.
  • the pyrolyzing can include heating the first material using a resistive heating member, such as a metal filament or metal ribbon. The heating can occur by direct contact between the resistive heating member and the first material.
  • the pyrolyzing can include heating the first material by induction, such as by using a Currie-Point pyrolyzer.
  • the pyrolyzing can include heating the first material by the application of radiation, such as infrared radiation.
  • the radiation can be generated by a laser, such as an infrared laser.
  • the pyrolyzing can include heating the first material with a convective heat.
  • the convective heat can be generated by a flowing stream of heated gas.
  • the heated gas can be maintained at a temperature of less than about 1200 °C, such as less than 1000 °C, less than 750 °C, less than 600 °C, less than 400 °C or even less than 300 °C.
  • the heated gas can be maintained at a temperature of greater than about 250 °C.
  • the convective heat can be generated by a hot body surrounding the first material, such as in a furnace.
  • the pyrolyzing can include heating the first material with steam at a temperature above about 250 °C.
  • Methods include oxidizing a first material that includes cellulose having a first number average molecular weight and having a first oxygen content to provide a second material that includes cellulose having a second number average molecular weight and having a second oxygen content higher than the first oxygen content.
  • the second material can be combined with a resin, e.g., a molten thermoplastic resin, to provide a composite.
  • a higher level of oxidation, while maintaining molecular weight, can provide composites with exceptional mechanical properties, such as improved abrasion resistance, compression strength, fracture resistance, impact strength, bending strength, tensile modulus, flexural modulus and elongation at break.
  • the second material can also be combined with any solid and/or liquid described herein, or any solid and/or liquid described in any patent application, patent or publication incorporated by reference herein.
  • the resin can include a component that includes hydrogen-bonding groups, such as one or more anhydride groups, carboxylic acid groups, hydroxyl groups, amide groups, amine groups or mixtures of any of these groups.
  • the component includes a polymer copolymerized with and/or grafted with maleic anhydride. Such materials are available from Dupont under the tradename FUSABOND ® .
  • the first material can be or can include, e.g., paper, paper products, wood, wood-related materials, particle board, grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, rice hulls, coconut hair, cotton, synthetic celluloses or mixtures of any of these materials.
  • Other materials that include cellulose are described herein. Still other materials that include cellulose are described in the patents, patent applications and publications that have been incorporated by reference herein.
  • the first material is in the form of a fibrous material that includes fibers.
  • fibrous materials can be, e.g., provided by shearing a fiber source, such as by shearing a fiber source using a rotary knife cutter.
  • the fibers of the fibrous material have an average length-to-diameter ratio of greater than 5/1.
  • the first and/or second material have a BET surface area of greater than 0.25 m 2 /g and/or a porosity of greater than about 25 percent.
  • the oxidizing can include pyrolyzing the first material by heating the first material using a resistive heating member, such as a metal filament or metal ribbon, in a oxidizing environment, such as in the presence of air, an oxygen-enriched inert gas (e.g., argon), or oxygen itself.
  • a resistive heating member such as a metal filament or metal ribbon
  • an oxygen-enriched inert gas e.g., argon
  • oxygen itself oxygen itself.
  • the heating occurs by direct contact between the resistive heating member and the first material.
  • oxidizing includes pyrolyzing the first material by heating the first material by induction, such as by a Currie-Point pyrolyzer, in an oxidizing environment.
  • oxidizing includes pyrolyzing the first material by heating the first material by the application of radiation, such as infrared radiation, in an oxidizing environment.
  • the radiation is generated by an infrared laser.
  • oxidizing includes pyrolyzing the first material by heating the first material with a convective heat in an oxidizing environment.
  • the convective heat can be generated by a flowing stream of heated gas.
  • the heated gas can be maintained at a temperature of less than about 1200 °C, such as less than 1000 °C, less than 750 °C, less than 600 °C, less than 400 °C or even less than 300 °C.
  • the convective heat is generated by a hot body surrounding the first material.
  • the oxidizing includes pyrolyzing the first material by heating the first material with steam at a temperature above about 250 °C.
  • Oxidation of the materials can be aided by still other techniques, including sonication.
  • the oxidizing can include sonicating the first material in an oxidizing environment.
  • the sonication can be performed while the first material is dispersed in an aqueous medium.
  • the sonication is performed using sound having a frequency of from about 12 kHz to about 25 kHz.
  • Oxidation of the materials can be performed by still other techniques, including ionizing and/or non-ionizing radiation.
  • the oxidizing can include irradiating the first material with gamma rays in an oxidizing environment and/or irradiating the first material with a beam of electrons in an oxidizing environment.
  • the second number average molecular weight is not more than fifteen percent lower than the first number average molecular weight. In some embodiments for providing composites, the second number average molecular weight is substantially the same as the first number average molecular weight.
  • the second oxygen content is at least about five percent higher than the first oxygen content, or even more preferably, twenty percent higher than the first oxygen content.
  • Methods include shearing a fiber source to provide a first fibrous material that includes cellulose having a first number average molecular weight and having a first oxygen content.
  • the first fibrous material is oxidized to provide a second fibrous material that includes cellulose having a second number average molecular weight and having a second oxygen content higher than the first oxygen content.
  • the second fibrous material can be utilized to make composites or it can be utilized for other applications.
  • the second material can be combined with any solid and/or liquid described herein, or any solid and/or liquid described in any patent application, patent or publication incorporated by reference herein.
  • the methods can further include combining the second fibrous material with a resin, such as a thermoplastic or thermosetting resin.
  • a resin such as a thermoplastic or thermosetting resin.
  • Methods include oxidizing a fiber source that includes cellulose having a first number average molecular weight and having a first oxygen content to provide an oxidized fiber source that includes cellulose having a second number average molecular weight and having a second oxygen content higher than the first oxygen content.
  • the oxidized fiber source is then sheared to provide an oxidized fibrous material that includes fibers.
  • the oxidized fibrous material can be utilized to make composites or it can be utilized for other applications.
  • the second material can be combined with any solid and/or liquid described herein, or any solid and/or liquid described in any patent application, patent or publication incorporated by reference herein.
  • Methods include oxidizing a first material that includes cellulose having a first number average molecular weight and having a first oxygen content to provide a second material that includes cellulose having a second number average molecular weight and having a second oxygen content higher than the first oxygen content.
  • the second fibrous material is densified to provide a densified fibrous material.
  • these methods can further include combining the densified fibrous material with a resin.
  • the methods further include fiberization of the densified fibrous material to provide a third fibrous material, and then combining the third fibrous material with a resin, such as a thermoplastic resin.
  • the densified or third fibrous material can be also combined with any solid and/or liquid described herein, or any solid and/or liquid described in any patent application, patent or publication incorporated by reference herein.
  • Methods include converting a first material that includes cellulose having a first number average molecular weight and having a first oxygen content to a second material that includes cellulose having a second number average molecular weight and having a second oxygen content higher than the first oxygen content; and combining the second material with a resin to provide a composite material.
  • the first and/or second material can also be combined with any solid and/or liquid described herein, or any solid and/or liquid described in any patent application, patent or publication incorporated by reference herein.
  • Methods include oxidizing a first material that includes cellulose having a first number average molecular weight and having a first oxygen content to provide a second material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight and having a second oxygen content higher than the first oxygen content; and combining the second material with a microorganism.
  • the microorganism can utilize the second material, e.g., by fermentation, to produce a fuel, such as hydrogen, alcohols, organic acids and hydrocarbons or mixtures of any of these fuels.
  • the first material is combined as well.
  • Methods include converting a first material that includes cellulose having a first number average molecular weight and having a first oxygen content to a second material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight and having a second oxygen content higher than the first oxygen content; and combining the second material with a solid and/or a liquid, such as a liquid that includes a microorganism, and/or an enzyme.
  • the first material is combined as well.
  • the microorganism utilizes the second material to produce a fuel, such as hydrogen, alcohols, organic acids and hydrocarbons or mixtures of any of these fuels.
  • the first material can also be utilized by the microorganism to produce a fuel.
  • a microorganism When a microorganism is utilized, it can be a natural microorganism or an engineered microorganism.
  • the microorganism can be a bacterium, e.g., a cellulolytic bacterium, a fungus, e.g., a yeast, a plant or a protist, e.g., an algae, a protozoa or a fungus-like protist, e.g., a slime mold.
  • the organisms are compatible, mixtures may be utilized.
  • various microorganisms can produce a number of useful products, such as a fuel, by operating on, e.g., fermenting the materials. For example, alcohols, organic acids, hydrocarbons, hydrogen, proteins or mixtures of any of these materials can be produced by fermentation or other processes.
  • Methods include shearing and steam exploding a fiber source to form a fibrous material; and contacting the fibrous material with a microorganism to produce a product.
  • useful products include hydrogen, alcohols, organic acids, hydrocarbons, proteins, and combinations thereof.
  • useful fiber sources include cellulosic material, lignocellulosic material, and combinations thereof.
  • Shearing and steam exploding the fiber source to form the fibrous material may be performed in any order.
  • multiple shearing and/or steam exploding operations may be performed in any order.
  • Shearing may be performed, for example, using a rotary knife cutter.
  • the fiber source may be cut prior to shearing and/or steam exploding.
  • the method includes shearing the fiber source to form a sheared fiber source, and then steam exploding the sheared fiber source to form the fibrous material. It is also possible to produce fibrous material by additionally shearing the steam exploded, sheared fiber source. It is also possible to shear the fiber source a second time to produce a second sheared fiber source, which is then steam exploded to produce the fibrous material.
  • Methods include steam exploding the fiber source to form a steam exploded fiber source, and then shearing the steam exploded fiber source to produce the fibrous material. It is also possible to produce fibrous material by additionally steam exploding the sheared, steam exploded fiber source.
  • Methods include shearing and steam exploding the fiber source concurrently to produce the fibrous material.
  • the method may include passing sheared material through one or more screens, e.g., a screen having an average opening size of 1.59 mm or less (0.0625 inch). Screening separates the material according to size.
  • the method includes: shearing the fiber source to produce a sheared fiber source; passing the sheared fiber source through a first screen to produce a screened fiber source; shearing the screened fiber source to produce a second sheared fiber source; passing the second sheared fiber source through a second screen having an average opening size less than the first screen to provide a second screened fiber source; and steam exploding the second screened fiber source to produce the fibrous material.
  • the method may further include shearing the second screened fiber source to produce a third sheared fiber source, and then steam exploding the third sheared fibers source to produce the fibrous material.
  • the methods may also further include encapsulating the fibrous material in a substantially gas impermeable material to remove entrapped gas and densify the fibrous material.
  • the substantially gas impermeable material may be soluble in water, and may be provided in the form of a bag.
  • microorganisms examples include bacteria, yeasts, enzymes, or combinations thereof.
  • the microorganism can be a bacterium, e.g., a cellulolytic bacterium, a fungus, e.g., a yeast, a plant or a protist, e.g., an algae, a protozoa or a fungus-like protist, e.g., a slime mold.
  • Examples of products that may be produced include mono- and polyfunctional C1-C6 alkyl alcohols, mono- and poly-functional carboxylic acids, C1-C6 hydrocarbons, and combinations thereof.
  • suitable alcohols include methanol, ethanol, propanol, isopropanol, butanol, ethylene glycol, propylene glycol, 1,4-butane diol, glycerin, and combinations thereof.
  • carboxylic acids include formic acid, acetic acid, propionic acid, butyric acid, valeric acid, caproic acid, palmitic acid, stearic acid, oxalic acid, malonic acid, succinic acid, glutaric acid, oleic acid, linoleic acid, glycolic acid, lactic acid, ⁇ -hydroxybutyric acid, and combinations thereof.
  • suitable hydrocarbons include methane, ethane, propane, pentane, n-hexane, and combinations thereof. Many of these products may be used as fuels.
  • microorganisms that may be used to produce useful products include bacteria, yeasts, or combinations thereof.
  • the microorganism can be a bacterium, e.g., a cellulolytic bacterium, a fungus, e.g., a yeast, a plant or a protist, e.g., an algae, a protozoa or a fungus-like protist, e.g., a slime mold.
  • Examples of products that may be produced include mono- and polyfunctional C1-C6 alkyl alcohols, mono- and poly-functional carboxylic acids, C1-C6 hydrocarbons, and combinations thereof.
  • suitable alcohols include methanol, ethanol, propanol, isopropanol, butanol, ethylene glycol, propylene glycol, 1,4-butane diol, glycerin, and combinations thereof.
  • carboxylic acids include formic acid, acetic acid, propionic acid, butyric acid, valeric acid, caproic acid, palmitic acid, stearic acid, oxalic acid, malonic acid, succinic acid, glutaric acid, oleic acid, linoleic acid, glycolic acid, lactic acid, ⁇ -hydroxybutyric acid, and combinations thereof.
  • suitable hydrocarbons include methane, ethane, propane, pentane, n-hexane, and combinations thereof. Many of these products may be used as fuels.
  • fibrous material is a material that includes numerous loose, discrete and separable fibers.
  • a fibrous material can be prepared from a bleached Kraft paper fiber source by shearing, e.g., with a rotary knife cutter.
  • screen means a member capable of sieving material according to size. Examples of screens include a perforated plate, cylinder or the like, or a wire mesh or cloth fabric.
  • pyrolysis means to break bonds in a material by the application of heat energy. Pyrolysis can occur while the subject material is under vacuum, or immersed in a gaseous material, such as an oxidizing gas, e.g., air or oxygen, or a reducing gas, such as hydrogen.
  • a gaseous material such as an oxidizing gas, e.g., air or oxygen, or a reducing gas, such as hydrogen.
  • Oxygen content is measured by elemental analysis by pyrolyzing a sample in a furnace operating at 1300 °C or above.
  • biomass refers to any non-fossilized, i.e., renewable, organic matter.
  • plant biomass defined below
  • animal biomass any animal by-product, animal waste, etc.
  • municipal waste biomass residential and light commercial refuse with recyclables such as metal and glass removed.
  • Plant biomass and "lingocellulosic biomass” refer to virtually any plant-derived organic matter (woody or non-woody) available for energy on a sustainable basis.
  • Plant biomass can include, but is not limited to, agricultural crop wastes and residues such as corn stover, wheat straw, rice straw, sugar cane bagasse, and the like.
  • Plant biomass further includes, but is not limited to, trees, woody energy crops, wood wastes and residues such as softwood forest thinnings, barky wastes, sawdust, paper and pulp industry waste streams, wood fiber, and the like. Additionally grass crops, such as switchgrass and the like have potential to be produced on a large-scale as another plant biomass source.
  • the best potential plant biomass feedstock includes yard waste (e.g., grass clippings, leaves; tree clippings, and brush) and vegetable processing waste.
  • "Lignocellulosic feedstock” is any type of plant biomass such as, but not limited to, non-woody plant biomass, cultivated crops, such as, but not limited to, grasses, for example, but not limited to, C4 grasses, such as switchgrass, cord grass, rye grass, miscanthus, reed canary grass, or a combination thereof, or sugar processing residues such as bagasse, or beet pulp, agricultural residues, for example, soybean stover, corn stover, rice straw, rice hulls, barley straw, corn cobs, wheat straw, canola straw, rice straw, oat straw, oat hulls, corn fiber, recycled wood pulp fiber, sawdust, hardwood, for example aspen wood and sawdust, softwood, or a combination thereof.
  • the lignocellulosic feedstock may include cell
  • Lignocellulosic feedstock may include one species of fiber or alternatively, lignocellulosic feedstock may include a mixture of fibers that originate from different lignocellulosic feedstocks. Furthermore, the lignocellulosic feedstock may comprise fresh lignocellulosic feedstock, partially dried lignocellulosic feedstock, fully dried lignocellulosic feedstock or a combination thereof.
  • carbohydrates are materials that are composed entirely of one or more saccharide units or that include one or more saccharide units.
  • Carbohydrates can be polymeric (e.g., equal to or greater than 10-mer, 100-mer, 1,000-mer, 10,000-mer, or 100,000-mer), oligomeric (e.g., equal to or greater than a 4-mer, 5-mer, 6-mer, 7-mer, 9-mer, 9-mer or 10-mer), trimeric, dimeric, or monomeric.
  • each repeat unit can be the same or different.
  • polymeric carbohydrates examples include cellulose, xylan, pectin, and starch, while cellobiose and lactose are examples of dimeric carbohydrates.
  • monomeric carbohydrates examples include glucose and xylose.
  • Carbohydrates can be part of a supramolecular structure, e.g., covalently bonded into the structure.
  • examples of such materials include lignocellulosic materials, such as that found in wood.
  • a combustible fuel is a material capable of burning in the presence of oxygen.
  • Examples of combustible fuels include ethanol, n-propanol, n-butanol, hydrogen and mixtures of any two or more of these.
  • Swelling agents as used herein are materials that cause a discernable swelling, e.g., a 2.5 percent increase in volume over an unswollen state of cellulosic and/or lignocellulosic materials, when applied to such materials as a solution, e.g., a water solution.
  • alkaline substances such as sodium hydroxide, potassium hydroxide, lithium hydroxide and ammonium hydroxides
  • acidifying agents such as mineral acids (e.g., sulfuric acid, hydrochloric acid and phosphoric acid)
  • salts such as zinc chloride, calcium carbonate, sodium carbonate, benzyltrimethylammonium sulfate, and basic organic amines, such as ethylene diamine.
  • a sheared material is a material that includes discrete fibers in which at least about 50% of the discrete fibers, have a length/diameter (L/D) ratio of at least about 5, and that has an uncompressed bulk density of less than about 0.6 g/cm 3 .
  • a sheared material is thus different from a material that has been cut, chopped or ground.
  • Changing a molecular structure of a biomass feedstock means to change the chemical bonding arrangement or conformation of the structure.
  • the change in the molecular structure can include changing the supramolecular structure of the material, oxidation of the material, changing an average molecular weight, changing an average crystallinity, changing a surface area, changing a degree of polymerization, changing a porosity, changing a degree of branching, grafting on other materials, changing a crystalline domain size, or an changing an overall domain size.
  • Biomass e.g., plant biomass, animal biomass, and municipal waste biomass
  • feedstock materials such as cellulosic and/or lignocellulosic materials that are readily available, but can be difficult to process, for example, by fermentation.
  • Feedstock materials are first physically prepared for processing, often by size reduction of raw feedstock materials. Physically prepared feedstock can be pretreated or processed using one or more of radiation, sonication, oxidation, pyrolysis, and steam explosion. The various pretreatment systems and methods can be used in combinations of two, three, or even four of these technologies.
  • feedstocks that include one or more saccharide units can be treated by any one or more of the processes described herein.
  • Other products and co-products that can be produced include, for example, human food, animal feed, pharmaceuticals, and nutriceuticals.
  • any biomass material that is or includes carbohydrates composed entirely of one or more saccharide units or that include one or more saccharide units can be processed by any of the methods described herein.
  • the biomass material can be cellulosic or lignocellulosic materials.
  • such materials can include paper, paper products, wood, wood-related materials, particle board, grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, rice hulls, coconut hair, algae, seaweed, cotton, synthetic celluloses, or mixtures of any of these.
  • Fiber sources include cellulosic fiber sources, including paper and paper products (e.g., polycoated paper and Kraft paper), and lignocellulosic fiber sources, including wood, and wood-related materials, e.g., particle board.
  • Other suitable fiber sources include natural fiber sources, e.g., grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, rice hulls, coconut hair, fiber sources high in ⁇ -cellulose content, e.g., cotton; and synthetic fiber sources, e.g., extruded yam (oriented yarn or un-oriented yam).
  • Natural or synthetic fiber sources can be obtained from virgin scrap textile materials, e.g., remnants or they can be post consumer waste, e.g., rags.
  • virgin materials e.g., scrap virgin materials, or they can be post-consumer waste.
  • industrial e.g., offal
  • processing waste e.g., effluent from paper processing
  • the fiber source can be obtained or derived from human (e.g., sewage), animal or plant wastes. Additional fiber sources have been described in U.S. Patent Nos. 6,448,307, 6,258,876, 6,207,729, 5,973,035 and 5,952,105.
  • the carbohydrate is or includes a material having one or more ⁇ -1,4-linkages and having a number average molecular weight between about 3,000 and 50,000.
  • a carbohydrate is or includes cellulose (I), which is derived from ( ⁇ -glucose 1) through condensation of ⁇ (1 ⁇ 4)-glycosidic bonds. This linkage contrasts itself with that for ⁇ (1 ⁇ 4)-glycosidic bonds present in starch and other carbohydrates.
  • Blends of any of the above materials may also be used.
  • FIG. 1 shows a system 100 for converting biomass, particularly biomass with significant cellulosic and lignocellulosic components, into useful products and co-products.
  • System 100 includes a feed preparation subsystem 110, a pretreatment subsystem 114, a primary process subsystem 118, and a post-processing subsystem 122.
  • Feed preparation subsystem 110 receives biomass in its raw form physically prepares the biomass for use as feedstock by downstream processes (e.g., reduces the size of and homogenizes the biomass), and stores the biomass both in its raw and feedstock forms.
  • Biomass feedstock with significant cellulosic and lignocellulosic components can have a high average molecular weight and crystallinity that can make processing the feedstock into useful products (e.g., fermenting the feedstock to produce ethanol) difficult.
  • Pretreatment subsystem 114 receives feedstock from the feed preparation subsystem 110 and prepares the feedstock for use in primary production processes by, for example, reducing the average molecular weight and crystallinity of the feedstock.
  • Primary process subsystem 118 receives pretreated feedstock from pretreatment subsystem 114 and produces useful products (e.g., ethanol, other alcohols, pharmaceuticals, and/or food products). In some cases, the output of primary process subsystem 118 is directly useful but, in other cases, requires further processing provided by post-processing subsystem 122.
  • Post-processing subsystem 122 provides further processing to product streams from primary process system 118 which require it (e.g., distillation and denaturation of ethanol) as well as treatment for waste streams from the other subsystems.
  • the cuts of subsystems 114,118,122 can also be directly or indirectly useful as secondary products and/or in increasing the overall efficiency of system 100.
  • post-processing subsystem 122 can produce treated water to be recycled for use as process water in other subsystems and/or can produce burnable waste which can be used as fuel for boilers producing steam and/or electricity.
  • the optimum size for biomass conversion plants is affected by factors including economies of scale and the type and availability of biomass used as feedstock. Increasing plant size tends to increase economies of scale associated with plant processes. However, increasing plant size also tends to increase the costs (e.g., transportation costs) per unit of feedstock. Studies analyzing these factors suggest that the appropriate size for biomass conversion plants can range from 2000 to 10,000 dried tons of feedstock per day depending at least in part on the type of feedstock used.
  • the type of feedstock can also impact plant storage requirements with plants designed primarily for processing feedstock whose availability varies seasonally (e.g., corn stower) requiring more on- or of-site feedstock storage than plants designed to process feedstock whose availability is relatively steady (e.g., waste paper).
  • methods of processing begin with a physical preparation of the feedstock, e.g., size reduction of raw feedstock materials, such as by cutting, grinding, shearing or chopping.
  • loose feedstock e.g., recycled paper or switchgrass
  • Screens and/or magnets can be used to remove oversized or undesirable objects such as, for example, rocks or nails from the feed stream.
  • Feed preparation systems can be configured to produce feed streams with specific characteristics such as, for example, specific maximum sizes, specific length-to-width, or specific surface areas ratios.
  • specific characteristics such as, for example, specific maximum sizes, specific length-to-width, or specific surface areas ratios.
  • the bulk density of feedstocks can be controlled (e.g., increased).
  • a fiber source 210 is sheared, e.g., in a rotary knife cutter, to provide a first fibrous material 212.
  • the first fibrous material 212 is passed through a first screen 214 having an average opening size of 1.59 mm or less (1/16 inch, 0.0625 inch) to provide a second fibrous material 216.
  • fiber source can be cut prior to the shearing, e.g., with a shredder.
  • the paper when a paper is used as the fiber source, the paper can be first cut into strips that are, e.g., 1/4- to 1/2-inch wide, using a shredder, e.g., a counter-rotating screw shredder, such as those manufactured by Munson (Utica, N.Y).
  • a shredder e.g., a counter-rotating screw shredder, such as those manufactured by Munson (Utica, N.Y).
  • the paper can be reduced in size by cutting to a desired size using a guillotine cutter.
  • the guillotine cutter can be used to cut the paper into sheets that are, e.g., 10 inches wide by 12 inches long.
  • the shearing of fiber source and the passing of the resulting first fibrous material through first screen are performed concurrently.
  • the shearing and the passing can also be performed in a batch-type process.
  • a rotary knife cutter can be used to concurrently shear the fiber source and screen the first fibrous material.
  • a rotary knife cutter 220 includes a hopper 222 that can be loaded with a shredded fiber source 224 prepared by shredding fiber source.
  • Shredded fiber source is sheared between stationary blades 230 and rotating blades 232 to provide a first fibrous material 240.
  • First fibrous material 240 passes through screen 242, and the resulting second fibrous material 244 is captured in bin 250.
  • the bin can have a pressure below nominal atmospheric pressure, e.g., at least 10 percent below nominal atmospheric pressure, e.g., at least 25 percent below nominal atmospheric pressure, at least 50 percent below nominal atmospheric pressure, or at least 75 percent below nominal atmospheric pressure.
  • a vacuum source 252 is utilized to maintain the bin below nominal atmospheric pressure.
  • Shearing can be advantageous for "opening up” and “stressing" the fibrous materials, making the cellulose of the materials more susceptible to chain scission and/or reduction of crystallinity.
  • the open materials can also be more susceptible to oxidation when irradiated.
  • the fiber source can be sheared in a dry state, a hydrated state (e.g., having up to ten percent by weight absorbed water), or in a wet state, e.g., having between about 10 percent and about 75 percent by weight water.
  • the fiber source can even be sheared while partially or fully submerged under a liquid, such as water, ethanol, isopropanol.
  • the fiber source can also be sheared in under a gas (such as a stream or atmosphere of gas other than air), e.g., oxygen or nitrogen, or steam.
  • a gas such as a stream or atmosphere of gas other than air
  • oxygen or nitrogen e.g., oxygen or nitrogen, or steam.
  • fibrous materials include, e.g., stone grinding, mechanical ripping or tearing, pin grinding or air attrition milling.
  • the fibrous materials can be separated, e.g., continuously or in batches, into fractions according to their length, width, density, material type, or some combination of these attributes. For example, for forming composites, it is often desirable to have a relatively narrow distribution of fiber lengths.
  • ferrous materials can be separated from any of the fibrous materials by passing a fibrous material that includes a ferrous material past a magnet, e.g., an electromagnet, and then passing the resulting fibrous material through a series of screens, each screen having different sized apertures.
  • a magnet e.g., an electromagnet
  • the fibrous materials can irradiated immediately following their preparation, or they can may be dried, e.g., at approximately 105 °C for 4-18 hours, so that the moisture content is, e.g., less than about 0.5% before use.
  • lignin can be removed from any of the fibrous materials that include lignin. Also, to aid in the breakdown of the materials that include the cellulose, the material can be treated prior to irradiation with heat, a chemical (e.g., mineral acid, base or a strong oxidizer such as sodium hypochlorite) and/or an enzyme.
  • a chemical e.g., mineral acid, base or a strong oxidizer such as sodium hypochlorite
  • an enzyme e.g., sodium hypochlorite
  • the average opening size of the first screen is less than 0.79 mm (1/32 inch, 0.03125 inch), e.g., less than 0.51 mm (1/50 inch, 0.02000 inch), less than 0.40 mm (1/64 inch, 0.015625 inch), less than 0.23 mm (0.009 inch), less than 0.20 mm (1/128 inch, 0.0078125 inch), less than 0.18 mm (0.007 inch), less than 0.13 mm (0.005 inch), or even less than less than 0.10 mm (1/256 inch, 0.00390625 inch).
  • the screen is prepared by interweaving monofilaments having an appropriate diameter to give the desired opening size.
  • the monofilaments can be made of a metal, e.g., stainless steel.
  • the screens can be advantageous to make the screens from monofilaments made from a material other than stainless steel, e.g., titanium, titanium alloys, amorphous metals, nickel, tungsten, rhodium, rhenium, ceramics, or glass.
  • the screen is made from a plate, e.g. a metal plate, having apertures, e.g., cut into the plate using a laser.
  • the open area of the mesh is less than 52%, e.g., less than 41%, less than 36%, less than 31%, less than 30%.
  • the second fibrous is sheared and passed through the first screen, or a different sized screen. In some embodiments, the second fibrous material is passed through a second screen having an average opening size equal to or less than that of first screen.
  • a third fibrous material 220 can be prepared from the second fibrous material 216 by shearing the second fibrous material 216 and passing the resulting material through a second screen 222 having an average opening size less than the first screen 214.
  • the fibers of the fibrous materials can have a relatively large average length-to-diameter ratio (e.g., greater than 20-to-1), even if they have been sheared more than once.
  • the fibers of the fibrous materials described herein may have a relatively narrow length and/or length-to-diameter ratio distribution.
  • average fiber widths are those determined optically by randomly selecting approximately 5,000 fibers.
  • Average fiber lengths are corrected length-weighted lengths.
  • BET Brunauer, Emmet and Teller
  • surface areas are multi-point surface areas, and porosities are those determined by mercury porosimetry.
  • the average length-to-diameter ratio of the second fibrous material 14 can be, e.g. greater than 8/1, e.g., greater than 10/1, greater than 15/1, greater than 20/1, greater than 25l1, or greater than 50/1.
  • An average length of the second fibrous material 14 can be, e.g., between about 0.5 mm and 2.5 mm, e.g., between about 0.75 mm and 1.0 mm, and an average width (i.e., diameter) of the second fibrous material 14 can be, e.g., between about 5 ⁇ m and 50 ⁇ m, e.g., between about 10 ⁇ m and 30 ⁇ m.
  • a standard deviation of the length of the second fibrous material 14 is less than 60 percent of an average length of the second fibrous material 14, e.g., less than 50 percent of the average length, less than 40 percent of the average length, less than 25 percent of the average length, less than 10 percent of the average length, less than 5 percent of the average length, or even less than 1 percent of the average length.
  • a BET surface area of the second fibrous material is greater than 0.1 m 2 /g, e.g., greater than 0.25 m 2 /g, greater than 0.5 m 2 /g, greater than 1.0 m 2 /g, greater than 1.5 m 2 /g, greater than 1.75 m 2 /g, greater than 5.0 m 2 /g, greater than 10 m 2 /g, greater than 25 m 2 /g, greater than 35 m 2 /g, greater than 50m 2 /g, greater than 60 m 2 /g, greater than 75 m 2 /g, greater than 100 m 2 /g, greater than 150 m 2 /g, greater than 200 m 2 /g, or even greater than 250 m 2 /g.
  • a porosity of the second fibrous material 14 can be, e.g., greater than 20 percent, greater than 25 percent, greater than 35 percent, greater than 50 percent, greater than 60 percent, greater than 70 percent, e.g., greater than 80 percent, greater than 85 percent, greater than 90 percent, greater than 92 percent, greater than 94 percent, greater than 95 percent, greater than 97.5 percent, greater than 99 percent, or even greater than 99.5 percent.
  • a ratio of the average length-to-diameter ratio of the first fibrous material to the average length-to-diameter ratio of the second fibrous material is, e.g., less than 1.5, e.g., less than 1.4, less than 1.25, less than 1.1, less than 1.075, less than 1.05, less than 1.025, or even substantially equal to 1.
  • the second fibrous material is sheared again and the resulting fibrous material passed through a second screen having an average opening size less than the first screen to provide a third fibrous material.
  • a ratio of the average length-to-diameter ratio of the second fibrous material to the average length-to-diameter ratio of the third fibrous material can be, e.g., less than 1.5, e.g., less than 1.4, less than 1.25, or even less than 1.1.
  • the third fibrous material is passed through a third screen to produce a fourth fibrous material.
  • the fourth fibrous material can be, e.g., passed through a fourth screen to produce a fifth material. Similar screening processes can be repeated as many times as desired to produce the desired fibrous material having the desired properties.
  • Densified materials can be processed by any of the methods described herein.
  • a material e.g., a fibrous material, having a low bulk density can be densified to a product having a higher bulk density.
  • a material composition having a bulk density of 0.05 g/ cm 3 can be densified by sealing the fibrous material in a relatively gas impermeable structure, e.g., a bag made of polyethylene or a bag made of alternating layers of polyethylene and a nylon, and then evacuating the entrapped gas, e.g., air, from the structure.
  • the fibrous material can have, e.g., a bulk density of greater than 0.3 g/cm 3 , e.g., 0.5 g/cm 3 , 0.6 g/cm 3 , 0.7 g/cm 3 or more, e.g., 0.85 g/ cm 3 .
  • the product can processed by any of the methods described herein, e.g., irradiated, e.g., with gamma radiation. This can be advantageous when it is desirable to transport the material to another location, e.g., a remote manufacturing plant, where the fibrous material composition can be added to a solution, e.g., to produce ethanol.
  • the densified fibrous material After piercing the substantially gas impermeable structure, the densified fibrous material can revert to nearly its initial bulk density, e.g., greater than 60 percent of its initial bulk density, e.g., 70 percent, 80 percent, 85 percent or more, e.g., 95 percent of its initial bulk density.
  • an anti-static agent can be added to the material.
  • the structure e.g., bag
  • the structure is formed of a material that dissolves in a liquid, such as water.
  • the structure can be formed from a polyvinyl alcohol so that it dissolves when in contact with a water-based system.
  • densified structures allow densified structures to be added directly to solutions that include a microorganism, without first releasing the contents of the structure, e.g., by cutting.
  • a biomass material can be combined with any desired additives and a binder, and subsequently densified by application of pressure, e.g., by passing the material through a nip defined between counter-rotating pressure rolls or by passing the material through a pellet mill.
  • pressure e.g., by passing the material through a nip defined between counter-rotating pressure rolls or by passing the material through a pellet mill.
  • heat can optionally be applied to aid in the densification of the fibrous material
  • the densified material can then be irradiated.
  • the material prior to densification has a bulk density of less than 0.25 g/cm 3 , e.g., 0.20 g/cm 3 , 0.15 g/cm 3 , 0.10 g/cm 3 , 0.05 g/cm 3 or less, e.g., 0.025 g/cm 3 .
  • Bulk density is determined using ASTM D1895B. Briefly, the method involves filling a measuring cylinder of known volume with a sample and obtaining a weight of the sample. The bulk density is calculated by dividing the weight of the sample in grams by the known volume of the cylinder in cubic centimeters.
  • the preferred binders include binders that are soluble in water, swollen by water, or that has a glass transition temperature of less 25 °C, as determined by differential scanning calorimetry.
  • water-soluble binders we mean binders having a solubility of at least about 0.05 weight percent in water.
  • water swellable binders we mean binders that increase in volume by more than 0.5 percent upon exposure to water.
  • the binders that are soluble or swollen by water include a functional group that is capable of forming a bond, e.g., a hydrogen bond, with the fibers of the fibrous material, e.g., cellulosic fibrous material.
  • the functional group can be a carboxylic acid group, a carboxylate group, a carbonyl group, e.g., of an aldehyde or a ketone, a sulfonic acid group, a sulfonate group, a phosphoric acid group, a phosphate group, an amide group, an amine group, a hydroxyl group, e.g., of an alcohol, and combinations of these groups, e.g., a carboxylic acid group and a hydroxyl group.
  • Specific monomeric examples include glycerin, glyoxal, ascorbic acid, urea, glycine, pentaerythritol, a monosaccharide or a disaccharide, citric acid, and tartaric acid.
  • Suitable saccharides include glucose, sucrose, lactose, ribose, fructose, mannose, arabinose and ecythrose.
  • Polymeric examples include polyglycols, polyethylene oxide, polycarboxylic acids, polyamides, polyamines and polysulfonic acids polysulfonates.
  • polymeric examples include polypropylene glycol (PPG), polyethylene glycol (PEG), polyethylene oxide, e.g., POLYOX ® , copolymers of ethylene oxide and propylene oxide, polyacrylic acid (PAA), polyacrylamide, polypeptides, polyethylenimine, polyvinylpyridine, poly(sodium-4-styrenesulfonate) and poly(2-acrylamidomethyl-1-propanesulfonic acid).
  • PPG polypropylene glycol
  • PEG polyethylene glycol
  • POLYOX ® polyethylene oxide
  • PAA polyacrylic acid
  • PAA polyacrylamide
  • polypeptides polyethylenimine
  • polyvinylpyridine poly(sodium-4-styrenesulfonate)
  • poly(2-acrylamidomethyl-1-propanesulfonic acid) poly(2-acrylamidomethyl-1-propanesulfonic acid).
  • the binder includes a polymer that has a glass transition temperature less 25 °C.
  • polymers include thermoplastic elastomers (TPEs).
  • TPEs include polyether block amides, such as those available under the tradename PEBAX ® , polyester elastomers, such as those available under the tradename HYTREL ® , and styrenic block copolymers, such as those available under the tradename KRATON ® .
  • Suitable polymers having a glass transition temperature less 25 °C include ethylene vinyl acetate copolymer (EVA), polyolefins, e.g., polyethylene, polypropylene, ethylene-propylene copolymers, and copolymers of ethylene and alpha olefins, e.g., 1-octene, such as those available under the tradename ENGAGE ® .
  • EVA ethylene vinyl acetate copolymer
  • polyolefins e.g., polyethylene, polypropylene, ethylene-propylene copolymers
  • copolymers of ethylene and alpha olefins e.g., 1-octene, such as those available under the tradename ENGAGE ® .
  • the material is a fiberized polycoated paper, the material is densified without the addition of a separate low glass transition temperature polymer.
  • the binder is a lignin, e.g., a natural or synthetically modified lignin.
  • a suitable amount of binder added to the material, calculated on a dry weight basis, is, e.g., from about 0.01 percent to about 50 percent, e.g., 0.03 percent, 0.05 percent, 0.1 percent, 0.25 percent, 0.5 percent, 1.0 percent, 5 percent, 10 percent or more, e.g., 25 percent, based on a total weight of the densified material.
  • the binder can be added to the material as a neat, pure liquid, as a liquid having the binder dissolved therein, as a dry powder of the binder, or as pellets of the binder.
  • the densified fibrous material can be made in a pellet mill.
  • a pellet mill 300 has a hopper 301 for holding undensified material 310 that includes a carbohydrate-containing materials, such as cellulose.
  • the hopper communicates with an auger 312 that is driven by variable speed motor 314 so that undensified material can be transported to a conditioner 320 that stirs the undensified material with paddles 322 that are rotated by conditioner motor 330.
  • Other ingredients e.g., any of the additives and/or fillers described herein, can be added at inlet 332. If desired, heat may be added while the fibrous material is in conditioner.
  • the material passes from the conditioner through a dump chute 340, and to another auger 342.
  • the dump chute as controlled by actuator 344, allows for unobstructed passage of the material from conditioner to auger.
  • Auger is rotated by motor 346, and controls the feeding of the fibrous material into die and roller assembly 350.
  • the material is introduced into a hollow, cylindrical die 352, which rotates about a horizontal axis and which has radially extending die holes 250. Die 352 is rotated about the axis by motor 360, which includes a horsepower gauge, indicating total power consumed by the motor.
  • Densified material 370 e.g., in the form of pellets, drops from chute 372 and are captured and processed, such as by irradiation.
  • the material after densification, can be conveniently in the form of pellets or chips having a variety of shapes.
  • the pellets can then be irradiated.
  • the pellets or chips are cylindrical in shape, e.g., having a maximum transverse dimension of, e.g., 1 mm or more, e.g., 2 mm, 3 mm, 5 mm, 8 mm, 10 mm, 15 mm or more, e.g., 25 mm.
  • Another convenient shape for making composites includes pellets or chips that are plate-like in form, e.g., having a thickness of 1 mm or more, e.g., 2 mm, 3 mm, 5 mm, 8 mm, 10 mm or more, e.g., 25 mm; a width of, e.g., 5 mm or more, e.g., 10 mm, 15 mm, 25 mm, 30 mm or more, e.g., 50 mm; and a length of 5 mm or more, e.g., 10 mm, 15 mm, 25 mm, 30 mm or more, e.g., 50 mm.
  • pellets can be made so that they have a hollow inside. As shown, the hollow can be generally in-line with the center of the pellet ( FIG. 7B ), or out of line with the center of the pellet ( FIG 7C ). Making the pellet hollow inside can increase the rate of dissolution in a liquid after irradiation.
  • the pellet can have, e.g., a transverse shape that is multilobal, e.g., tri-lobal as shown, or tetra-lobal, penta-lobal, hexa-lobal or deca-lobal. Making the pellets in such transverse shapes can also increase the rate of dissolution in a solution after irradiation.
  • a transverse shape that is multilobal, e.g., tri-lobal as shown, or tetra-lobal, penta-lobal, hexa-lobal or deca-lobal.
  • half-gallon juice cartons made of un-printed white Kraft board having a bulk density of 20 lb/ft 3 can be used as a feedstock.
  • Cartons can be folded flat and then fed into a shredder to produce a confetti-like material having a width of between 0.1 inch and 0.5 inch, a length of between 0.25 inch and 1 inch and a thickness equivalent to that of the starting material (about 0.075 inch).
  • the confetti-like material can be fed to a rotary knife cutter which shears the confetti-like pieces, tearing the pieces apart and releasing fibrous material.
  • multiple shredder-shearer trains can be arranged in series with output.
  • two shredder-shearer trains can be arranged in series with output from the first shearer fed as input to the second shredder.
  • three shredder-shearer trains can be arranged in series with output from the first shearer fed as input to the second shredder and output from the second shearer fed as input to the third shredder. Multiple passes through shredder-shearer trains are anticipated to increase decrease particle size and increase overall surface area within the feedstream.
  • fibrous material produced from shredding and shearing juice cartons can be treated to increase its bulk density.
  • the fibrous material can be sprayed with water or a dilute stock solution of POLYOX TM WSR N10 (polyethylene oxide) prepared in water.
  • POLYOX TM WSR N10 polyethylene oxide
  • the wetted fibrous material can then be processed through a pellet mill operating at room temperature. The pellet mill can increase the bulk density of the feedstream by more than an order of magnitude.
  • Physically prepared feedstock can be pretreated for use in primary production processes by, for example, reducing the average molecular weight and crystallinity of the feedstock and/or increasing the surface area and/or porosity of the feedstock
  • Pretreatment processes can include one or more of irradiation, sonication, oxidation, pyrolysis, and steam explosion.
  • the various pretreatment systems and methods can be used in combinations of two, three, or even four of these technologies.
  • biomass can be processed by applying two or more of any of the processes described herein, such as two or more of radiation, sonication, oxidation, pyrolysis, and steam explosion either with or without prior, intermediate, or subsequent feedstock preparation as described herein.
  • the processes can be applied in any order (or concurrently) to the biomass, e.g., a cellulosic and/or lignocellulosic material.
  • materials that include a carbohydrate are prepared by applying three, four or more of any of the processes described herein (in any order or concurrently).
  • a carbohydrate can be prepared by applying radiation, sonication, oxidation, pyrolysis, and, optionally, steam explosion to a cellulosic and/or lignocellulosic material (in any order or concurrently).
  • the provided carbohydrate-containing material can then be converted by one or more microorganisms, such as bacteria, yeast, or mixtures of yeast and bacteria, to a number of desirable products, as described herein.
  • microorganisms such as bacteria, yeast, or mixtures of yeast and bacteria
  • feedstocks include a carbohydrate that is produced by a process that includes irradiating and sonicating (in either order or concurrently) a cellulosic and/or a lignocellulosic material, a process that includes irradiating and oxidizing (in either order or concurrently) a cellulosic and/or a lignocellulosic material, a process that includes irradiating and pyrolyzing (in either order or concurrently) a cellulosic and/or a lignocellulosic material, a process that includes irradiating and pyrolyzing (in either order or concurrently) a cellulosic and/or a lignocellulosic material, or a process that includes irradiating and steam-exploding (in either order or concurrently) a cellulosic and/or a lignocellulosic material.
  • the provided feedstock can then be contacted with a microorganism having the ability to convert at least a portion, e.g., at least about 1 percent by weight, of the feedstock to the product, such as the combustible fuel, as described herein.
  • the process does not include hydrolyzing the cellulosic and/or lignocellulosic material, such as with an acid or a base, e.g., a mineral acid, such as hydrochloric or sulfuric acid.
  • an acid or a base e.g., a mineral acid, such as hydrochloric or sulfuric acid.
  • some or none of the feedstock can include a hydrolyzed material.
  • a hydrolyzed material for example, in some embodiments, at least about seventy percent by weight of the feedstock is an unhydrolyzed material, e.g., at least at 95 percent by weight of the feedstock is an unhydrolyzed material. In some embodiments, substantially all of the feedstock is an unhydrolyzed material.
  • Any feedstock or any reactor or fermentor charged with a feedstock can include a buffer, such as sodium bicarbonate, ammonium chloride or Tris; an electrolyte, such as potassium chloride, sodium chloride, or calcium chloride; a growth factor, such as biotin and/or a base pair such as uracil or an equivalent thereof; a surfactant, such as Tween ® or polyethylene glycol; a mineral, such as such as calcium, chromium, copper, iodine, iron, selenium, or zinc; or a chelating agent, such as ethylene diamine, ethylene diamine tetraacetic acid (EDTA) (or its salt form, e.g., sodium or potassium EDTA), or dimercaprol.
  • a buffer such as sodium bicarbonate, ammonium chloride or Tris
  • an electrolyte such as potassium chloride, sodium chloride, or calcium chloride
  • a growth factor such as biotin and/or a base pair such as
  • irradiation can be performed on cellulosic and/or lignocellulosic material in which less than about 25 percent by weight of the cellulosic and/or lignocellulosic material has surfaces wetted with a liquid, such as water.
  • irradiating is performed on cellulosic and/or lignocellulosic material in which substantially none of the cellulosic and/or lignocellulosic material is wetted with a liquid, such as water.
  • any processing described herein occurs after the cellulosic and/or lignocellulosic material remains dry as acquired or has been dried, e.g., using heat and/or reduced pressure.
  • the cellulosic and/or lignocellulosic material has less than about five percent by weight retained water, measured at 25°C and at fifty percent relative humidity.
  • a swelling agent can be utilized in any process described herein.
  • a cellulosic and/or lignocellulosic material when a cellulosic and/or lignocellulosic material is processed using radiation, less than about 25 percent by weight of the cellulosic and/or lignocellulosic material is in a swollen state, the swollen state being characterized as having a volume of more than about 2.5 percent higher than an unswollen state, e.g., more than 5.0, 7.5, 10, or 15 percent higher than the unswollen state.
  • radiation when radiation is utilized on a cellulosic and/or lignocellulosic material, substantially none of the cellulosic and/or lignocellulosic material is in a swollen state.
  • the cellulosic and/or lignocellulosic material when radiation is utilized, includes a swelling agent, and swollen cellulosic and/or lignocellulosic receives a dose of less than about 10 Mrad.
  • the cellulosic and/or lignocellulosic When radiation is utilized in any process, it can be applied while the cellulosic and/or lignocellulosic is exposed to air, oxygen-enriched air, or even oxygen itself, or blanketed by an inert gas such as nitrogen, argon, or helium.
  • an oxidizing environment is utilized, such as air or oxygen.
  • biomass such as cellulosic and/or lignocellulosic material
  • a pressure of greater than about 2.5 atmospheres such as greater than 5, 10, 15, 20 or even greater than about 50 atmospheres.
  • the process includes irradiating and sonicating and irradiating precedes sonicating. In other specific embodiments, sonication precedes irradiating, or irradiating and sonicating occur concurrently.
  • the process includes irradiating and sonicating (in either order or concurrently) and further includes oxidizing, pyrolyzing or steam exploding.
  • the irradiating can be performed utilizing an ionizing radiation, such as gamma rays, x-rays, energetic ultraviolet radiation, such as ultraviolet C radiation having a wavelength of from about 100 nm to about 280 nm, a beam of particles, such as a beam of electrons, slow neutrons or alpha particles.
  • irradiating includes two or more radiation sources, such as gamma rays and a beam of electrons, which can be applied in either order or concurrently.
  • sonicating can performed at a frequency of between about 15khz and about 25khz, such as between about 18khz and 22khz utilizing a 1 KW or larger horn, e.g., a 2, 3, 4, 5, or even a 10 KW horn.
  • the cellulosic and/or lignocellulosic material includes a first cellulose having a first number average molecular weight and the resulting carbohydrate includes a second cellulose having a second number average molecular weight lower than the first number average molecular weight.
  • the second number average molecular weight is lower than the first number average molecular weight by more than about twenty-five percent, e.g., 2x, 3x, 5x, 7x, 10x 25x, even 100x reduction.
  • the first cellulose has a first crystallinity and the second cellulose has a second crystallinity lower than the first crystallinity, such as lower than about two, three, five, ten, fifteen or twenty-five percent lower.
  • the first cellulose has a first level of oxidation and the second cellulose has a second level of oxidation higher than the first level of oxidation, such as two, three, four, five, ten or even twenty-five percent higher.
  • half-gallon juice cartons made of un-printed polycoated white Kraft board having a bulk density of 20 lb/ft 3 are used as a feedstock.
  • Cartons are folded flat and then fed into a sequence of three shredder-shearer trains arranged in series with output from the first shearer fed as input to the second shredder, and output from the second shearer fed as input to the third shredder.
  • the fibrous material produced by the can be sprayed with water and processed through a pellet mill operating at room temperature.
  • the densified pellets can be placed in a glass ampoule which is sealed under an atmosphere of air.
  • the pellets in the ampoule are irradiated with gamma radiation for about 3 hours at a dose rate of about 1 Mrad per hour to provide an irradiated material in which the cellulose has a lower molecular weight than the fibrous Kraft starting material.
  • One or more irradiation processing sequences can be used to process raw feedstock from a wide variety of different sources to extract useful substances from the feedstock, and to provide partially degraded organic material which functions as input to further processing steps and/or sequences. Irradiation can reduce the molecular weight and/or crystallinity of feedstock.
  • energy deposited in a material that releases an electron from its atomic orbital is used to irradiate the materials.
  • the radiation may be provided by 1) heavy charged particles, such as alpha particles, 2) electrons, produced, for example, in beta decay or electron beam accelerators, or 3) electromagnetic radiation, for example, gamma rays, x rays, or ultraviolet rays.
  • radiation produced by radioactive substances can be used to irradiate the feedstock.
  • electromagnetic radiation e.g., produced using electron beam emitters
  • the doses applied depend on the desired effect and the particular feedstock. For example, high doses of radiation can break chemical bonds within feedstock components and low doses of radiation can increase chemical bonding (e.g., cross-linking) within feedstock components.
  • a first material 2 that is or includes cellulose having a first number average molecular weight ( T M N1 ) is irradiated, e.g., by treatment with ionizing radiation (e.g., in the form of gamma radiation, X-ray radiation, 100 mn to 280 nm ultraviolet (UV) light, a beam of electrons or other charged particles) to provide a second material 3 that includes cellulose having a second number average molecular weight ( T M N2 ) lower than the first number average molecular weight.
  • ionizing radiation e.g., in the form of gamma radiation, X-ray radiation, 100 mn to 280 nm ultraviolet (UV) light, a beam of electrons or other charged particles
  • the second material (or the first and second material) can be combined with a microorganism (e.g., a bacterium or a yeast) that can utilize the second and/or first material to produce a fuel 5 that is or includes hydrogen, an alcohol (e.g., ethanol or butanol, such as n-, sec- or t-butanol), an organic acid, a hydrocarbon or mixtures of any of these.
  • a microorganism e.g., a bacterium or a yeast
  • a microorganism e.g., a bacterium or a yeast
  • the second material 3 Since the second material 3 has cellulose having a reduced molecular weight relative to the first material, and in some instances, a reduced crystallinity as well, the second material is generally more dispersible, swellable and/or soluble in a solution containing a microorganism. These properties make the second material 3 more susceptible to chemical, enzymatic and/or biological attack relative to the first material 2, which can greatly improve the production rate and/or production level of a desired product, e.g., ethanol. Radiation can also sterilize the materials.
  • the second number average molecular weight (M N2 ) is lower than the first number average molecular weight ( T M N1 ) by more than about 10 percent, e.g., 15, 20, 25, 30, 35, 40, 50 percent, 60 percent, or even more than about 75 percent
  • the second material has cellulose that has as crystallinity ( T C 2 ) that is lower than the crystallinity ( T C 1 ) of the cellulose of the first material.
  • ( T C 2 ) can be lower than ( T C 1 ) by more than about 10 percent, e.g., 15, 20, 25, 30, 35, 40, or even more than about 50 percent.
  • the starting crystallinity index (prior to irradiation) is from about 40 to about 87.5 percent, e.g., from about 50 to about 75 percent or from about 60 to about 70 percent, and the crystallinity index after irradiation is from about 10 to about 50 percent, e.g., from about 15 to about 45 percent or from about 20 to about 40 percent.
  • the material after irradiation is substantially amorphous.
  • the starting number average molecular weight (prior to irradiation) is from about 200,000 to about 3,200,000, e.g., from about 250,000 to about 1,000,000 or from about 250,000 to about 700,000, and the number average molecular weight after irradiation is from about 50,000 to about 200,000, e.g., from about 60,000 to about 150,000 or from about 70,000 to about 125,000.
  • the number average molecular weight is less than about 10,000 or even less than about 5,000.
  • the second material can have a level of oxidation ( T O 2 ) that is higher than the level of oxidation ( T O 1 ) of the first material.
  • T O 2 a level of oxidation
  • T O 1 the level of oxidation of the first material.
  • a higher level of oxidation of the material can aid in its dispersability, swellability and/or solubility, further enhancing the materials susceptibility to chemical, enzymatic or biological attack.
  • the irradiation is performed under an oxidizing environment, e.g., under a blanket of air or oxygen, producing a second material that is more oxidized than the first material.
  • the second material can have more hydroxyl groups, aldehyde groups, ketone groups, ester groups or carboxylic acid groups, which can increase its hydrophilicity.
  • Each form of radiation ionizes the biomass via particular interactions, as determined by the energy of the radiation.
  • Heavy charged particles primarily ionize matter via Coulomb scattering; furthermore, these interactions produce energetic electrons that may further ionize matter.
  • Alpha particles are identical to the nucleus of a helium atom and are produced by the alpha decay of various radioactive nuclei, such as isotopes of bismuth, polonium, astatine, radon, francium, radium, several actinides, such as actinium, thorium, uranium, neptunium, curium, californium, americium, and plutonium.
  • Electrons interact via Coulomb scattering and bremssthrahlung radiation produced by changes in the velocity of electrons. Electrons may be produced by radioactive nuclei that undergo beta decay, such as isotopes of iodine, cesium, technetium, and iridium. Alternatively, an electron gun can be used as an electron source via thermionic emission.
  • Electromagnetic radiation interacts via three processes: photoelectric absorption, Compton scattering, and pair production.
  • the dominating interaction is determined by the energy of the incident radiation and the atomic number of the material.
  • the summation of interactions contributing to the absorbed radiation in cellulosic material can be expressed by the mass absorption coefficient, graphed below as a function of incident energy.
  • Electromagnetic radiation is subclassified as gamma rays, x rays, ultraviolet rays, infrared rays, microwaves, or radiowaves, depending on its wavelength.
  • a gamma irradiator 10 includes gamma radiation sources 408, e.g., 60 Co pellets, a working table 14 for holding the materials to be irradiated and storage 16, e.g., made of a plurality iron plates, all of which are housed in a concrete containment chamber 20 that includes a maze entranceway 22 beyond a lead-lined door 26.
  • Storage 16 includes a plurality of channels 30, e.g., sixteen or more channels, allowing the gamma radiation sources to pass through storage on their way proximate the working table.
  • the sample to be irradiated is placed on a working table.
  • the irradiator is configured to deliver the desired dose rate and monitoring equipment is connected to an experimental block 31.
  • the operator then leaves the containment chamber, passing through the maze entranceway and through the lead-lined door.
  • the operator mans a control panel 32, instructing a computer 33 to lift the radiation sources 12 into working position using cylinder 36 attached to a hydraulic pump 40.
  • Gamma radiation has the advantage of a significant penetration depth into a variety of material in the sample.
  • Sources of gamma rays include radioactive nuclei, such as isotopes of cobalt, calcium, technicium, chromium, gallium, indium, iodine, iron, krypton, samarium, selenium, sodium, thalium, and xenon.
  • Sources of x rays include electron beam collision with metal targets, such as tungsten or molybdenum or alloys, or compact light sources, such as those produced commercially by Lyncean.
  • Sources for ultraviolet radiation include deuterium or cadmium lamps.
  • Sources for infrared radiation include sapphire, zinc, or selenide window ceramic lamps.
  • Sources for microwaves include klystrons, Slevin type RF sources, or atom beam sources that employ hydrogen, oxygen, or nitrogen gases.
  • a beam of electrons is used as the radiation source.
  • a beam of electrons has the advantages of high dose rates (e.g., 1, 5, or even 10 Mrad per second), high throughput, less containment, and less confinement equipment. Electrons can also be more efficient at causing chain scission. In addition, electrons having energies of 4-10 MeV can have a penetration depth of 5 to 30 mm or more, such as 40 mm.
  • Electron beams can be generated, e.g., by electrostatic generators, cascade generators, transformer generators, low energy accelerators with a scanning system, low energy accelerators with a linear cathode, linear accelerators, and pulsed accelerators. Electrons as an ionizing radiation source can be useful, e.g., for relatively thin piles of materials, e.g., less than 0.5 inch, e.g., less than 0.4 inch, 0.3 inch, 0.2 inch, or less than 0.1 inch.
  • the energy of each electron of the electron beam is from about 0.3 MeV to about 2.0 MeV (million electron volts), e.g., from about 0.5 MeV to about 1.5 MeV, or from about 0.7 MeV to about 1.25 MeV.
  • FIG. 11 shows a process flow diagram 3000 that includes various steps in an electron beam irradiation feedstock pretreatment sequence.
  • first step 3010 a supply of dry feedstock is received from a feed source.
  • the dry feedstock from the feed source may be pre-processed prior to delivery to the electron beam irradiation devices.
  • the biomass feedstock can be subjected to mechanical processing (e.g., to reduce the average length of fibers in the feedstock) prior to delivery to the electron beam irradiation devices.
  • step 3030 the dry feedstock is transferred to a feedstock transport device (e.g., a conveyor belt) and is distributed over the cross-sectional width of the feedstock transport device approximately uniformly by volume. This can be accomplished, for example, manually or by inducing a localized vibration motion at some point in the feedstock transport device prior to the electron beam irradiation processing.
  • a feedstock transport device e.g., a conveyor belt
  • a mixing system introduces a chemical agent 3045 into the feedstock in an optional process 3040 that produces a slurry.
  • a chemical agent 3045 into the feedstock in an optional process 3040 that produces a slurry.
  • Combining water with the processed feedstock in mixing step 3040 creates an aqueous feedstock slurry that may be transported through, for example, piping rather than using, for example, a conveyor belt.
  • the next step 3050 is a loop that encompasses exposing the feedstock (in dry or slurry form) to electron beam radiation via one or more (say, N) electron beam irradiation devices.
  • the feedstock slurry is moved through each of the N "showers" of electron beams at step 3052.
  • the movement may either be at a continuous speed through and between the showers, or there may be a pause through each shower, followed by a sudden movement to the next shower.
  • a small slice of the feedstock slurry is exposed to each shower for some predetermined exposure time at step 3053.
  • Electron beam irradiation devices may be procured commercially from Ion Beam Applications, Louvain-la-Neuve, Belgium or the Titan Corporation, San Diego, CA.
  • Typical electron energies can be 1 MeV, 2 MeV, 4.5 MeV, 7.5 MeV, or 10 MeV.
  • Typical electron beam irradiation device power can be 1 kW, 5 kW, 10 kW, 20 kW, 50 kW, 100 kW, 250 kW, or 500 kW.
  • Effectiveness of depolymerization of the feedstock slurry depends on the electron energy used and the dose applied, while exposure time depends on the power and dose.
  • Typical doses may take values of 1 kGy, 5 kGy, 10 kGy, 20 kGy, 50 kGy, 100 kGy, or 200 kGy.
  • the feedstock transport device could direct the feedstock (in dry or slurry form) underneath and in a reverse direction to its initial transport direction.
  • Double-pass systems can allow thicker feedstock slurries to be processed and can provide a more uniform depolymerization through the thickness of the feedstock slurry.
  • the electron beam irradiation device can produce either a fixed beam or a scanning beam.
  • a scanning beam may be advantageous with large scan sweep length and high scan speeds, as this would effectively replace a large, fixed beam width. Further, available sweep widths of 0.5 m, 1m, 2 m or more are available.
  • step 3060 it may be necessary in some embodiments, as in step 3060, to mechanically separate the liquid and solid components of the feedstock slurry.
  • a liquid portion of the feedstock slurry is filtered for residual solid particles and recycled back to the slurry preparation step 3040.
  • a solid portion of the feedstock slurry is then advanced on to the next processing step 3070 via the feedstock transport device.
  • the feedstock is maintained in slurry form for further processing.
  • the electromagnetic radiation can have, e.g., energy per photon (in electron volts) of greater than 10 2 eV, e.g., greater than 10 3 , 10 4 , 10 5 , 10 6 , or even greater than 16 7 eV. In some embodiments, the electromagnetic radiation has energy per photon of between 10 4 and 10 7 , e.g., between 10 5 and 10 6 eV.
  • the electromagnetic radiation can have a frequency of, e.g., greater than 10 16 hz, greater than 10 17 hz, 10 18 , 10 19 , 10 20 , or even greater than 10 21 hz. In some embodiments, the electromagnetic radiation has a frequency of between 10 18 and 10 22 hz, e.g., between 10 19 to 10 21 hz.
  • the irradiating (with any radiation source or a combination of sources) is performed until the material receives a dose of at least 0.25 Mrad, e.g., at least 1.0 Mrad, at least 2.5 Mrad, at least 5.0 Mrad, or at least 10.0 Mrad. In some embodiments, the irradiating is performed until the material receives a dose of between 1.0 Mrad and 6.0 Mrad, e.g., between 1.5 Mrad and 4.0 Mrad.
  • the irradiating is performed at a dose rate of between 5.0 and 1500.0 kilorads/hour, e.g., between 10.0 and 750.0 kilorads/hour or between 50.0 and 350.0 kilorads/hours.
  • two or more radiation sources are used, such as two or more ionizing radiations.
  • samples can be treated, in any order, with a beam of electrons, followed by gamma radiation and UV light having wavelengths from about 100 nm to about 280 nm.
  • samples are treated with three ionizing radiation sources, such as a beam of electrons, gamma radiation, and energetic UV light.
  • relatively low doses of radiation can crosslink, graft, or otherwise increase the molecular weight of a carbohydrate-containing material, such as a cellulosic or lignocellulosic material (e.g., cellulose).
  • a carbohydrate-containing material such as a cellulosic or lignocellulosic material (e.g., cellulose).
  • a material having increased molecular weight can be useful, e.g., in making a composite, e.g., having improved mechanical properties, such as abrasion resistance, compression strength, fracture resistance, impact strength, bending strength, tensile modulus, flexural modulus and elongation at break.
  • Such a material having increased molecular weight can be useful in making a composition.
  • a fibrous material that includes a first cellulosic and/or lignocellulosic material having a first molecular weight can be irradiated in such a manner as to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight.
  • a dose of from about 1 Mrad to about 10 Mrad e.g., from about 1.5 Mrad to about 7.5 Mrad or from about 2.0 Mrad to about 5.0 Mrad, can be applied.
  • the second cellulosic and/or lignocellulosic material can be combined with a resin and formed into a composite, e.g., by compression molding, injection molding; or extrusion.
  • a resin e.g., by compression molding, injection molding; or extrusion.
  • Forming composites is described in WO 2006/102543 , and in U.S. Provisional Patent Application Serial Nos. 60/664,832, filed on March 24, 2005 , 60/688,002, filed on June 7, 2005 , 601711,057, filed on August 24, 2005 , 60/715,822, filed on September 9, 2005 , 60/725,674, filed on October 12, 2005 , 60/726,102, filed on October 12,2005 , and 60/750,205, filed on December 13,2005 .
  • a fibrous material that includes a first cellulosic and/or lignocellulosic material having a first molecular weight can be combined with a resin to provide a composite, and then the composite can be irradiated with a relatively low dose of radiation so as to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight.
  • a relatively low dose of radiation so as to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight.
  • gamma radiation is utilized as the radiation source
  • a dose of from about 1 Mrad to about 10 Mrad can be applied. Using this approach increases the molecular weight of the material while it is with a resin matrix.
  • the resin is a cross-linkable resin and as such it crosslinks as the carbohydrate-containing material increases in molecular weight, which can provide a synergistic effect to provide maximum mechanical properties to the composite.
  • such composites can have excellent low temperature performance, e.g., having a reduced tendency to break and/or crack at low temperatures, e.g., temperatures below 0 °C, e.g., below -10 °C, -20 °C, -40 °C, -50 °C, -60 °C or even below -100 °C, and/or excellent performance at high temperatures, e.g., capable of maintaining their advantageous mechanical properties at relatively high temperature, e.g., at temperatures above 100 °C, e.g., above 125 °C, 150 °C, 200 °C, 250 °C, 300 °C, 400 °C, or even above 500 °C.
  • such composites can have excellent chemical resistance, e.g., resistance to swelling in a solvent, e.g., a hydrocarbon solvent, resistance to chemical attack, e.g., by strong acids, strong bases, strong oxidants (e.g., chlorine or bleach) or reducing agents (e.g., active metals such as sodium and potassium).
  • a solvent e.g., a hydrocarbon solvent
  • chemical attack e.g., by strong acids, strong bases, strong oxidants (e.g., chlorine or bleach) or reducing agents (e.g., active metals such as sodium and potassium).
  • a fibrous material that includes a cellulosic and/or lignocellulosic material is irradiated and, optionally, treated with acoustic energy, e.g., ultrasound.
  • half-gallon juice cartons made of un-printed polycoated white Kraft board having a bulk density of 20 lb/ft 3 are used as a feedstock.
  • Cartons are folded flat and then fed into a sequence of three shredder-shearer trains arranged in series with output from the first shearer fed as input to the second shredder, and output from the second shearer fed as input to the third shredder.
  • the fibrous material produced by the can be sprayed with water and processed through a pellet mill operating at room temperature.
  • the densified pellets can be placed in a glass ampoule which is evacuated under high vacuum and then back-filled with argon gas. The ampoule is sealed under argon.
  • the pellets in the ampoule are irradiated with gamma radiation for about 3 hours at a dose rate of about 1 Mrad per hour to provide an irradiated material in which the cellulose has a lower molecular weight than the starting material.
  • One or more sonication processing sequences can be used to process raw feedstock from a wide variety of different sources to extract useful substances from the feedstock, and to provide partially degraded organic material which functions as input to further processing steps and/or sequences. Sonication can reduce the molecular weight and/or crystallinity of feedstock.
  • a first material 2 that includes cellulose having a first number average molecular weight ( T M N1 ) is dispersed in a medium, such as water, and sonicated and/or otherwise cavitated, to provide a second material 3 that includes cellulose having a second number average molecular weight ( T M N2 ) lower than the first number average molecular weight.
  • the second material (or the first and second material in certain embodiments) can be combined with a microorganism (e.g., a bacterium or a yeast) that can utilize the second and/or first material to produce a fuel 5 that is or includes hydrogen, an alcohol, an organic acid, a hydrocarbon or mixtures of any of these.
  • the second material Since the second material has cellulose having a reduced molecular weight relative to the first material, and in some instances, a reduced crystallinity as well, the second material is generally more dispersible, swellable, and/or soluble in a solution containing the microorganism, e.g., at a concentration of greater than 10 6 microorganisms/mL. These properties make the second material 3 more susceptible to chemical, enzymatic, and/or microbial attack relative to the first material 2, which can greatly improve the production rate and/or production level of a desired product, e.g., ethanol. Sonication can also sterilize the materials, but should not be used while the microorganisms are supposed to be alive.
  • a desired product e.g., ethanol.
  • the second number average molecular weight ( T M N2 ) is lower than the first number average molecular weight ( T M N1 ) by more than about 10 percent, e.g., 15, 20, 25, 30, 35, 40, 50 percent, 60 percent, or even more than about 75 percent.
  • the second material has cellulose that has as crystallinity ( T C 2 ) that is lower than the crystallinity ( T C 1 ) of the cellulose of the first material.
  • ( T C 2 ) can be lower than ( T C 1 ) by more than about 10 percent, e.g.,15, 20, 25, 30, 35, 40, or even more than about 50 percent.
  • the starting crystallinity index (prior to sonication) is from about 40 to about 87.5 percent, e.g., from about 50 to about 75 percent or from about 60 to about 70 percent, and the crystallinity index after sonication is from about 10 to about 50 percent, e.g., from about 15 to about 45 percent or from about 20 to about 40 percent
  • the material after sonication is substantially amorphous.
  • the starting number average molecular weight (prior to sonication) is from about 200,000 to about 3,200,000, e.g., from about 250,000 to about 1,000,000 or from about 250,000 to about 700,000, and the number average molecular weight after sonication is from about 50,000 to about 200,000, e.g., from about 60,000 to about 150,000 or from about 70,000 to about 125,000.
  • the number average molecular weight is less than about 10,000 or even less than about 5,000.
  • the second material can have a level of oxidation ( T O 2 ) that is higher than the level of oxidation ( T O 1 ) of the first material.
  • T O 2 a level of oxidation of the material
  • T O 1 the level of oxidation of the first material
  • the sonication is performed in an oxidizing medium, producing a second material that is more oxidized than the first material.
  • the second material can have more hydroxyl groups, aldehyde groups, ketone groups, ester groups or carboxylic acid groups, which can increase its hydrophilicity.
  • the sonication medium is an aqueous medium.
  • the medium can include an oxidant, such as a peroxide (e.g., hydrogen peroxide), a dispersing agent and/or a buffer.
  • oxidant such as a peroxide (e.g., hydrogen peroxide)
  • dispersing agents include ionic dispersing agents, e.g., sodium lauryl sulfate, and non-ionic dispersing agents, e.g., poly(ethylene glycol).
  • the sonication medium is non-aqueous.
  • the sonication can be performed in a hydrocarbon, e.g., toluene or heptane, an ether, e.g., diethyl ether or tetrahydrofuran, or even in a liquefied gas such as argon, xenon, or nitrogen.
  • sonication breaks bonds in the cellulose by creating bubbles in the medium containing the cellulose, which grow and then violently collapse.
  • the implosive force raises the local temperature within the bubble to about 5100 K (even higher in some instance; see, e.g., Suslick et al., Nature 434,52-55 ) and generates pressures of from a few hundred atmospheres to over 1000 atmospheres or more. It is these high temperatures and pressures that break the bonds.
  • reduced crystallinity arises, at least in part, from the extremely high cooling rates during collapse of the bubbles, which can be greater than about 10 11 K/second.
  • the high cooling rates generally do not allow the cellulose to organize and crystallize, resulting in materials that have reduced crystallinity.
  • Ultrasonic systems and sonochemistry are discussed in, e.g., Olli et al., U.S. Patent No. 5,766,764 ; Roberts, U.S. Patent No.
  • FIG. 12 shows a general system in which a cellulosic material stream 1210 is mixed with a water stream 1212 in a reservoir 1214 to form a process stream 1216.
  • a first pump 1218 draws process stream 1216 from reservoir 1214 and toward a flow cell 1224.
  • Ultrasonic transducer 1226 transmits ultrasonic energy into process stream 1216 as the process stream flows through flow cell 1224.
  • a second pump 1230 draws process stream 1216 from flow cell 1224 and toward subsequent processing.
  • Reservoir 1214 includes a first intake 1232 and a second intake 1234 in fluid communication with a volume 1236.
  • a conveyor (not shown) delivers cellulosic material stream 1210 to reservoir 1214 through first intake 1232.
  • Water stream 1212 enters reservoir 1214 through second intake 1234.
  • water stream 1212 enters volume 1236 along a tangent establishing a swirling flow within volume 1236.
  • FIG. 39 is a schematic view of a process for biomass conversion.
  • volume 1236 is introduced into volume 1236 along opposing axes to enhance mixing within the volume.
  • Valve 1238 controls the flow of water stream 1212 through second intake 1232 to produce a desired ratio of cellulosic material to water (e.g., approximately 10% cellulosic material, weight by volume). For example, 2000 tons/day of cellulosic material can be combined with 1 million to 1.5 million gallons/day, e.g., 1.25 million gallons/day, of water.
  • Reservoir 1214 includes a mixer 1240 in fluid communication with volume 1236.
  • Mixer 1240 agitates the contents of volume 1236 to disperse cellulosic material throughout the water in the volume.
  • mixer 1240 can be a rotating vane disposed in reservoir 1214.
  • mixer 1240 disperses the cellulosic material substantially uniformly throughout the water.
  • Reservoir 1214 further includes an exit 1242 in fluid communication with volume 1236 and process stream 1216.
  • the mixture of cellulosic material and water in volume 1236 flows out of reservoir 1214 via exit 1242.
  • Exit 1242 is arranged near the bottom of reservoir 1214 to allow gravity to pull the mixture of cellulosic material and water out of reservoir 1214 and into process stream 1216.
  • First pump 1218 moves the contents of process stream 1216 toward flow cell 1224.
  • first pump 1218 agitates the contents of process stream 1216 such that the mixture of cellulosic material and water is substantially uniform at inlet 1220 of flow cell 1224.
  • first pump 1218 agitates process stream 1216 to create a turbulent flow that persists along the process stream between the first pump and inlet 1220 of flow cell 1224.
  • Flow cell 1224 includes a reactor volume 1244 in fluid communication with inlet 1220 and outlet 1222.
  • reactor volume 1244 is a stainless steel tube capable of withstanding elevated pressures (e.g., 10 bars).
  • reactor volume 1244 includes a rectangular cross section.
  • Flow cell 1224 further includes a heat exchanger 1246 in thermal communication with at least a portion of reactor volume 1244.
  • Cooling fluid 1248 e.g., water
  • the flow rate of cooling fluid 1248 into heat exchanger 1246 is controlled to maintain an approximately constant temperature in reactor volume 1244.
  • the temperature of cooling fluid 1248 flowing into heat exchanger 1246 is controlled to maintain an approximately constant temperature in reactor volume 1244.
  • the temperature of reactor volume 1244 is maintained at 20 to 50°C, e.g., 25, 30, 35, 40, or 45°C. Additionally or alternatively, heat transferred to cooling fluid 1248 from reactor volume 1244 can be used in other parts of the overall process.
  • An adapter section 1226 creates fluid communication between reactor volume 1244 and a booster 1250 coupled (e.g., mechanically coupled using a flange) to ultrasonic transducer 1226.
  • adapter section 1226 can include a flange and O-ring assembly arranged to create a leak tight connection between reactor volume 1244 and booster 1250.
  • ultrasonic transducer 1226 is a high-powered ultrasonic transducer made by Hielscher Ultrasonics of Teltow, Germany.
  • a generator 1252 delivers electricity to ultrasonic transducer 1252.
  • Ultrasonic transducer 1226 includes a piezoelectric element that converts the electrical energy into sound in the ultrasonic range.
  • the materials are sonicated using sound having a frequency of from about 16 kHz to about 110 kHz, e.g., from about 18 kHz to about 75 kHz or from about 20 kHz to about 40 kHz. (e.g., sound having a frequency of 20 kHz to 40 kHz).
  • the ultrasonic energy is then delivered to the working medium through booster 1248.
  • the ultrasonic energy traveling through booster 1248 in reactor volume 1244 creates a series of compressions and rarefactions in process stream 1216 with an intensity sufficient to create cavitation in process stream 1216.
  • Cavitation disaggregates the cellulosic material dispersed in process stream 1216. Cavitation also produces free radicals in the water of process stream 1216. These free radicals act to further break down the cellulosic material in process stream 1216.
  • process stream 1216 has been described as a single flow path, other arrangements are possible.
  • process stream 1216 includes multiple parallel flow paths (e.g., flowing at a rate of 10 gallon/min).
  • the multiple parallel flow paths of process stream 1216 flow into separate flow cells and are sonicated in parallel (e.g., using a plurality of 16 kW ultrasonic transducers).
  • ultrasonic transducer 1226 has been described as being coupled to flow cell 1224, other arrangements are possible.
  • a plurality of ultrasonic transducers 1226 are arranged in flow cell 1224 (e.g., ten ultrasonic transducers can be arranged in a flow cell 1224).
  • the sound waves generated by each of the plurality of ultrasonic transducers 1226 are timed (e.g., synchronized out of phase with one another) to enhance the cavitation acting upon process stream 1216.
  • second pump 1230 moves process stream to a second flow cell where a second booster and ultrasonic transducer further sonicate process stream 1216.
  • reactor volume 1244 has been described as a closed volume
  • reactor volume 1244 is open to ambient conditions in certain embodiments.
  • sonication pretreatment can be performed substantially simultaneously with other pretreatment techniques.
  • ultrasonic energy can be applied to process stream 1216 in reactor volume 1244 while electron beams are simultaneously introduced into process stream 1216.
  • sonication can be performed in a batch process.
  • a volume can be filled with a 10% (weight by volume) mixture of cellulosic material in water and exposed to sound with intensity from about 50 W/cm 2 to about 600 W/cm 2 , e.g., from about 75 W/cm 2 to about 300 W/cm 2 or from about 95 W/cm 2 to about 200 W/cm 2 .
  • the mixture in the volume can be sonicated from about 1 hour to about 24 hours, e.g., from about 1.5 hours to about 12 hours, or from about 2 hours to about 10 hours.
  • the material is sonicated for a pre-determined time, and then allowed to stand for a second pre-determined time before sonicating again.
  • two electroacoustic transducers are mechanically coupled to a single horn.
  • a pair of piezoelectric transducers 60 and 62 is coupled to a slotted bar horn 64 by respective intermediate coupling horns 70 and 72, the latter also being known as booster horns.
  • the mechanical vibrations provided by the transducers, responsive to high frequency electrical energy applied thereto, are transmitted to the respective coupling horns, which may be constructed to provide a mechanical gain, such as a ratio of 1 to 1.2.
  • the horns are provided with a respective mounting flange 74 and 76 for supporting the transducer and horn assembly in a stationary housing.
  • the vibrations transmitted from the transducers through the coupling or booster horns are coupled to the input surface 78 of the horn and are transmitted through the horn to the oppositely disposed output surface 80, which, during operation, is in forced engagement with a workpiece (not shown) to which the vibrations are applied.
  • the high frequency electrical energy provided by the power supply 82 is fed to each of the transducers, electrically connected in parallel, via a balancing transformer 84 and a respective series connected capacitor 86 and 90, one capacitor connected in series with the electrical connection to each of the transducers.
  • the balancing transformer is known also as “balun” standing for “balancing unit.”
  • the balancing transformer includes a magnetic core 92 and a pair of identical windings 94 and 96, also termed the primary winding and secondary winding, respectively.
  • the transducers include commercially available piezoelectric transducers, such as Branson Ultrasonics Corporation models 105 or 502, each designed for operation at 20 kHz and a maximum power rating of 3 kW.
  • the energizing voltage for providing maximum motional excursion at the output surface of the transducer is 930 volt rms.
  • the current flow through a transducer may vary between zero and 3.5 ampere depending on the load impedance. At 930 volt rms the output motion is approximately 20 microns.
  • the maximum difference in terminal voltage for the same motional amplitude therefore, can be 186 volt. Such a voltage difference can give rise to large circulating currents flowing between the transducers.
  • the balancing unit 430 assures a balanced condition by providing equal current flow through the transducers, hence eliminating the possibility of circulating currents.
  • the wire size of the windings must be selected for the full load current noted above and the maximum voltage appearing across a winding input is 93 volt.
  • high-frequency, rotor-stator devices can be utilized. This type of device produces high-shear, microcavitation forces which can disintegrate biomass in contact with such forces.
  • Two commercially available high-frequency, rotor-stator dispersion devices are the Supraton TM devices manufactured by Krupp Industrietechnik GmbH and marketed by Dorr-Oliver GmbH of Connecticut, and the Dispax TM devices manufactured and marketed by Ika-Works, Inc. of Cincinnati, Ohio. Operation of such a microcavitation device is discussed in Stuart, U.S. Patent No. 5,370,999 .
  • ultrasonic transducer 1226 has been described as using the electromagnetic -response of magnetorestrictive materials to produce ultrasonic energy, other arrangements are possible.
  • acoustic energy in the form of an intense shock wave can be applied directly to process stream 16 using an underwater spark.
  • ultrasonic energy is transferred to process stream 16 through a thermohydraulic system.
  • acoustic waves of high energy density can be produced by applying power across an enclosed volume of electrolyte, thereby heating the enclosed volume and producing a pressure rise that is subsequently transmitted through a sound propagation medium (e.g., process stream 1216). Design and operation of such a thermohydraulic transducer is discussed in Hartmann et al., U.S. Patent 6,383,152 .
  • One or more pyrolysis processing sequences can be used to process raw feedstock from a wide variety of different sources to extract useful substances from the feedstock, and to provide partially degraded organic material which functions as input to further processing steps and/or sequences.
  • a first material 2 that includes cellulose having a first number average molecular weight ( T M N1 ) is pyrolyzed, e.g., by heating the first material in a tube furnace, to provide a second material 3 that includes cellulose having a second number average molecular weight ( T M N2 ) lower than the first number average molecular weight.
  • the second material (or the first and second material in certain embodiments) is/are combined with a microorganism (e.g., a bacterium or a yeast) that can utilize the second and/or first material to produce a fuel 5 that is or includes hydrogen, an alcohol (e.g., ethanol or butanol, such as n-, sec or t-butanol), an organic acid, a hydrocarbon or mixtures of any of these.
  • a microorganism e.g., a bacterium or a yeast
  • a microorganism e.g., a bacterium or a yeast
  • the second material Since the second material has cellulose having a reduced molecular weight relative to the first material, and in some instances, a reduced crystallinity as well, the second material is generally more dispersible, swellable and/or soluble in a solution containing the microorganism, e.g., at a concentration of greater than 10 6 microorganisms/mL. These properties make the second material 3 more susceptible to chemical, enzymatic and/or microbial attack relative to the first material 2, which can greatly improve the production rate and/or production level of a desired product, e.g., ethanol. Pyrolysis can also sterilize the first and second materials.
  • the second number average molecular weight ( T M N2 ) is lower than the first number average molecular weight ( T M N1 ) by more than about 10 percent, e.g.,15, 20, 25, 30, 35, 40, 50 percent, 60 percent, or even more than about 75 percent.
  • the second material has cellulose that has as crystallinity ( T C 2 ) that is lower than the crystallinity ( T C 1 ) of the cellulose of the first material.
  • ( T C 2 ) can be lower than ( T C 1 ) by more than about 10 percent, e.g.,15, 20, 25, 30, 35, 40, or even more than about 50 percent.
  • the starting crystallinity (prior to pyrolysis) is from about 40 to about 87.5 percent, e.g., from about 50 to about 75 percent or from about 60 to about 70 percent, and the crystallinity index after pyrolysis is from about 10 to about 50 percent, e.g., from about 15 to about 45 percent or from about 20 to about 40 percent.
  • the material after pyrolysis is substantially amorphous.
  • the starting number average molecular weight (prior to pyrolysis) is from about 200,000 to about 3,200,000, e.g., from about 250,000 to about 1,000,000 or from about 250,000 to about 700,000, and the number average molecular weight after pyrolysis is from about 50,000 to about 200,000, e.g., from about 60,000 to about 150,000 or from about 70,000 to about 125,000.
  • the number average molecular weight is less than about 10,000 or even less than about 5,000.
  • the second material can have a level of oxidation ( T O 2 ) that is higher than the level of oxidation ( T O 1 ) of the first material.
  • T O 2 a level of oxidation of the material
  • T O 1 the level of oxidation of the first material
  • the pyrolysis is performed in an oxidizing environment, producing a second material that is more oxidized than the first material.
  • the second material can have more hydroxyl groups, aldehyde groups, ketone groups, ester groups or carboxylic acid groups, which can increase its hydrophilicity.
  • the pyrolysis of the materials is continuous. In other embodiments, the material is pyrolyzed for a pro-determined time, and then allowed to cool for a second pre-determined time before pyrolyzing again.
  • FIG. 14 shows a process flow diagram 6000 that includes various steps in a pyrolytic feedstock pretreatment system.
  • first step 6010 a supply of dry feedstock is received from a feed source.
  • the dry feedstock from the feed source may be pre-processed prior to delivery to the pyrolysis chamber.
  • the feedstock is derived from plant sources, certain portions of the plant material may be removed prior to collection of the plant material and/or before the plant material is delivered by the feedstock transport device.
  • the biomass feedstock can be subjected to mechanical processing 6020 (e.g., to reduce the average length of fibers in the feedstock) prior to delivery to the pyrolysis chamber.
  • the feedstock undergoes a moisture adjustment step 6030.
  • the nature of the moisture adjustment step depends upon the moisture content of the mechanically processed feedstock. Typically, pyrolysis of feedstock occurs most efficiently when the moisture content of the feedstock is between about 10% and about 30% (e.g., between 15% and 25%) by weight of the feedstock. If the moisture content of the feedstock is larger than about 40% by weight, the extra thermal load presented by the water content of the feedstock increases the energy consumption of subsequent pyrolysis steps.
  • the mechanically processed feedstock can be combined with wetter feedstock material 6230 with a higher moisture content, such as sewage sludge.
  • water 6240 can be added to the dry feedstock from step 6020 to increase its moisture content.
  • step 6040 the feedstock - now with its moisture content adjusted to fall within suitable limits - can be preheated in an optional preheating step 6040.
  • Preheating step 6040 can be used to increase the temperature of the feedstock to between 75 °C and 150°C in preparation for subsequent pyrolysis of the feedstock.
  • preheating the feedstock can ensure that heat distribution within the feedstock remains more uniform during pyrolysis, and can reduce the thermal load on the pyrolysis chamber.
  • the feedstock is then transported to a pyrolysis chamber to undergo pyrolysis in step 6050.
  • transport of the feedstock is assisted by adding one or more pressurized gases 6210 to the feedstock stream.
  • the gases create a pressure gradient in a feedstock transport conduit, propelling the feedstock into the pyrolysis chamber (and even through the pyrolysis chamber).
  • transport of the feedstock occurs mechanically; that is, a transport system that includes a conveyor such as an auger transports the feedstock to the pyrolysis chamber.
  • gases 6210 can also be added to the feedstock prior to the pyrolysis chamber.
  • one or more catalyst gases can be added to the feedstock to assist decomposition of the feedstock during pyrolysis.
  • one or more scavenging agents can be added to the feedstock to trap volatile materials released during pyrolysis.
  • various sulfur-based compounds such as sulfides can be liberated during pyrolysis, and an agent such as hydrogen gas can be added to the feedstock to cause desulfurization of the pyrolysis products.
  • Hydrogen combines with sulfides to form hydrogen sulfide gas, which can be removed from the pyrolyzed feedstock.
  • Pyrolysis of the feedstock within the chamber can include heating the feedstock to relatively high temperatures to cause partial decomposition of the feedstock.
  • the feedstock is heated to a temperature in a range from 150 °C to 1100 °C.
  • the temperature to which the feedstock is heated depends upon a number of factors, including the composition of the feedstock, the feedstock average particle size, the moisture content, and the desired pyrolysis products. For many types of biomass feedstock, for example, pyrolysis temperatures between 300 °C and 550 °C are used.
  • the residence time of the feedstock within the pyrolysis chamber generally depends upon a number of factors, including the pyrolysis temperature, the composition of the feedstock, the feedstock average particle size, the moisture content, and the desired pyrolysis products.
  • feedstock materials are pyrolyzed at a temperature just above the decomposition temperature for the material in an inert atmosphere, e.g., from about 2°C above to about 10 °C above the decomposition temperature or from about 3 °C above to about 7 °C above the decomposition temperature.
  • the material is generally kept at this temperature for greater than 0.5 hours, e.g., greater than 1.0 hours or greater than about 2.0 hours.
  • the materials are pyrolyzed at a temperature well above the decomposition temperature for the material in an inert atmosphere, e.g., from about 75 °C above to about 175 °C above the decomposition temperature or from about 85 °C above to about 150 °C above the decomposition temperature.
  • the material is generally kept at this temperature for less than 0.5 hour, e.g., less 20 minutes, less than 10 minutes, less than 5 minutes or less than 2 minutes.
  • the materials are pyrolyzed at an extreme temperature, e.g., from about 200 °C above to about 500 °C above the decomposition temperature of the material in an inert environment or from about 250 °C above to about 400 °C above the decomposition temperature.
  • the material us generally kept at this temperature for less than 1 minute, e.g., less than 30 seconds, less than 15 seconds, less than 10 seconds, less than 5 seconds, less than 1 second or less than 500 ms.
  • flash pyrolysis Such embodiments are typically referred to as flash pyrolysis.
  • a turbulent flow of feedstock material within the pyrolysis chamber is usually advantageous, as it ensures relatively efficient heat transfer to the feedstock material from the heating sub-system.
  • Turbulent flow can be achieved by blowing the feedstock material through the chamber using one or more injected carrier gases 6210, for example.
  • the carrier gases are relatively inert towards the feedstock material, even at the high temperatures in the pyrolysis chamber.
  • Exemplary carrier gases include, for example, nitrogen, argon, methane, carbon monoxide, and carbon dioxide.
  • mechanical transport systems such as augers can transport and circulate the feedstock within the pyrolysis chamber to create a turbulent feedstock flow.
  • pyrolysis of the feedstock occurs substantially in the absence of oxygen and other reactive gases.
  • Oxygen can be removed from the pyrolysis chamber by periodic purging of the chamber with high pressure nitrogen (e.g., at nitrogen pressures of 2 bar or more).
  • a gas mixture present in the pyrolysis chamber e.g., during pyrolysis of the feedstock
  • can include less than 4 mole% oxygen e.g., less than 1 mole% oxygen, and even less than 0.5 mole% oxygen.
  • the absence of oxygen ensures that ignition of the feedstock does not occur at the elevated pyrolysis temperatures.
  • relatively small amounts of oxygen can be introduced into the feedstock and are present during pyrolysis.
  • This technique is referred to as oxidative pyrolysis.
  • oxidative pyrolysis occurs in multiple heating stages. For example, in a first heating stage, the feedstock is heated in the presence of oxygen to cause partial oxidation of the feedstock. This stage consumes the available oxygen in the pyrolysis chamber. Then, in subsequent heating stages, the feedstock temperature is further elevated. With all of the oxygen in the chamber consumed, however, feedstock combustion does not occur, and combustion-free pyrolytic decomposition of the feedstock (e.g., to generate hydrocarbon products) occurs.
  • the process of heating feedstock in the pyrolysis chamber to initiate decomposition is endothermic.
  • formation of carbon dioxide by oxidation of the feedstock is an exothermic process.
  • the heat released from carbon dioxide formation can assist further pyrolysis heating stages, thereby lessening the thermal load presented by the feedstock.
  • pyrolysis occurs in an inert environment, such as while feedstock materials are bathed in argon or nitrogen gas.
  • pyrolysis can occur in an oxidizing environment, such as in air or argon enriched in air.
  • pyrolysis can take place in a reducing environment, such as while feedstock materials are bathed in hydrogen gas.
  • various chemical agents such as oxidants, reductants, acids or bases can be added to the material prior to or during pyrolysis.
  • sulfuric acid can be added, or a peroxide (e.g., benzoyl peroxide) can be added.
  • a variety of different processing conditions can be used, depending upon factors such as the feedstock composition and the desired pyrolysis products.
  • relatively mild pyrolysis conditions can be employed, including flash pyrolysis temperatures between 375 °C and 450 °C, and residence times of less than 1 second.
  • flash pyrolysis temperatures between 500 °C and 650°C are typically used, with residence times of between 0.5 and 3 seconds.
  • quenching step 6250 includes spraying the pyrolysis products with streams of cooling water 6260.
  • the cooling water also forms a slurry that includes solid, undissolved product material and various dissolved products.
  • Also present in the product stream is a mixture that includes various gases, including product gases, carrier gases, and other types of process gases.
  • the product stream is transported via in-line piping to a gas separator that performs a gas separation step 6060, in which product gases and other gases are separated from the slurry formed by quenching the pyrolysis products.
  • the separated gas mixture is optionally directed to a blower 6130, which increases the gas pressure by blowing air into the mixture.
  • the gas mixture can be subjected to a filtration step 6140, in which the gas mixture passes through one or more filters (e.g., activated charcoal filters) to remove particulates and other impurities.
  • the filtered gas can be compressed and stored for further use.
  • the filtered gas can be subjected to further processing steps 6160.
  • the filtered gas can be condensed to separate different gaseous compounds within the gas mixture.
  • the different compounds can include, for example, various hydrocarbon products (e.g., alcohols, alkanes, alkenes, alkynes, ethers) produced during pyrolysis.
  • the filtered gas containing a mixture of hydrocarbon components can be combined with steam gas 6170 (e.g., a mixture of water vapor and oxygen) and subjected to a cracking process to reduce molecular weights of the hydrocarbon components.
  • the pyrolysis chamber includes heat sources that burn hydrocarbon gases such as methane, propane, and/or butane to heat the feedstock.
  • hydrocarbon gases such as methane, propane, and/or butane
  • a portion 6270 of the separated gases can be recirculated into the pyrolysis chamber for combustion, to generate process heat to sustain the pyrolysis process.
  • the pyrolysis chamber can receive process heat that can be used to increase the temperature of feedstock materials.
  • irradiating feedstock with radiation e.g., gamma radiation, electron beam radiation, or other types of radiation
  • the heated feedstock materials can be cooled by a beat exchange system that removes some of the excess heat from the irradiated feedstock.
  • the heat exchange system can be configured to transport some of the heat energy to the pyrolysis chamber to heat (or pre-heat) feedstock material, thereby reducing energy cost for the pyrolysis process.
  • the slurry containing liquid and solid pyrolysis products can undergo an optional dewatering step 6070, in which excess water can be removed from the slurry via processes such as mechanical pressing and evaporation.
  • the excess water 6280 can be filtered and then recirculated for further use in quenching the pyrolysis decomposition products in step 6250.
  • pyrolysis process parameters discussed above are exemplary. In general, values of these parameters can vary widely according to the nature of the feedstock and the desired products. Moreover, a wide variety of different pyrolysis techniques, including using heat sources such as hydrocarbon flames and/or furnaces, infrared lasers, microwave heaters, induction heaters, resistive heaters, and other heating devices and configurations can be used.
  • heat sources such as hydrocarbon flames and/or furnaces, infrared lasers, microwave heaters, induction heaters, resistive heaters, and other heating devices and configurations can be used.
  • pyrolyzing can include heating the material with a convective heat.
  • the convective heat can be generated by a flowing stream of heated gas.
  • the heated gas can be maintained at a temperature of less than about 1200 °C, such as less than 1000 °C, less than 750 °C, less than 600 °C, less than 400 °C or even less than 300 °C.
  • the heated gas can be maintained at a temperature of greater than about 250 °C.
  • the convective heat can be generated by a hot body surrounding the first material, such as in a furnace.
  • pyrolyzing can include heating the material with steam at a temperature above about 250 °C.
  • Chamber 6500 includes an insulated chamber wall 6510 with a vent 6600 for exhaust gases, a plurality of burners 6520 that generate heat for the pyrolysis process, a transport duct 6530 for transporting the feedstock through chamber 6500, augers 6590 for moving the feedstock through duct 6530 in a turbulent flow, and a quenching system 6540 that includes an auger 6610 for moving the pyrolysis products, water jets 6550 for spraying the pyrolysis products with cooling water, and a gas separator for separating gaseous products 6580 from a slurry 6570 containing solid and liquid products.
  • Chamber 6700 includes an insulated chamber wall 6710, a feedstock supply duct 6720, a sloped inner chamber wall 6730, burners 6740 that generate heat for the pyrolysis process, a vent 6750 for exhaust gases, and a gas separator 6760 for separating gaseous products 6770 from liquid and solid products 6780.
  • Chamber 6700 is configured to rotate in the direction shown by arrow 6790 to ensure adequate mixing and turbulent flow of the feedstock within the chamber.
  • a carrier gas e.g., an inert gas, or an oxidizing or reducing gas
  • a desired temperature e.g., 325°C.
  • the pyrolyzed material is emptied from the sample holder.
  • the system shown in FIG. 17 can be scaled and made continuous.
  • the heating member can be an auger screw. Material can continuously fall into the sample holder, striking a heated screw that pyrolizes the material. At the same time, the screw can push the pyrolyzed material out of the sample holder to allow for the entry of fresh, unpyrolyzed material.
  • FIG. 18 Another embodiment of a pyrolysis chamber is shown in FIG. 18 , which features a Curie-Point pyrolyzer 1820 that includes a sample chamber 1821 housing a ferromagnetic foil 1822. Surrounding the sample chamber 1821 is an RF coil 1823. The space 1824 defined by enclosure 1825 is maintained at a temperature above room temperature, e.g., 200 to 250°C. In a typical usage, a carrier gas traverses through the sample chamber 1821 while the foil 1822 is inductively heated by an applied RF field to pyrolize the material at a desired temperature.
  • a carrier gas traverses through the sample chamber 1821 while the foil 1822 is inductively heated by an applied RF field to pyrolize the material at a desired temperature.
  • Furnace pyrolyzer 130 includes a movable sample holder 131 and a furnace 132.
  • the sample is lowered (as indicated by arrow 137) into a hot zone 135 of furnace 132, while a carrier gas fills the housing 136 and traverses through the sample holder 131.
  • the sample is heated to the desired temperature for a desired time to provide a pyrolyzed product.
  • the pyrolyzed product is removed from the pyrolyzer by raising the sample holder (as indicated by arrow 134).
  • a cellulosic target 140 can be pyrolyzed by treating the target, which is housed in a vacuum chamber 141, with laser light, e.g., light having a wavelength of from about 225 nm to about 1500 nm.
  • the target can be ablated at 266 nm, using the fourth harmonic of a Nd-YAG laser (Spectra Physics, GCR170, San Jose, Calif.).
  • the optical configuration shown allows the nearly monochromatic light 143 generated by the laser 142 to be directed using mirrors 144 and 145 onto the target after passing though a lens 146 in the vacuum chamber 141.
  • a cellulosic material can be flash pyrolyzed by coating a tungsten filament 150, such as a 5 to 25 mil tungsten filament, with the desired cellulosic material while the material is housed in a vacuum chamber 151.
  • a tungsten filament 150 such as a 5 to 25 mil tungsten filament
  • current is passed through the filament, which causes a rapid heating of the filament for a desired time. Typically, the heating is continued for seconds before allowing the filament to cool. In some embodiments, the heating is performed a number of times to effect the desired amount of pyrolysis.
  • carbohydrate-containing biomass material can be heated in an absence of oxygen in a fluidized bed reactor.
  • the carbohydrate containing biomass can have relatively thin cross-sections, and can include any of the fibrous materials described herein, for efficient heat transfer.
  • the material can be heated by thermal transfer from a hot metal or ceramic, such as glass beads or sand in the reactor, and the resulting pyrolysis liquid or oil can be transported to a central refinery for making combustible fuels or other useful products.
  • One or more oxidative processing sequences can be used to process raw feedstock from a wide variety of different sources to extract useful substances from the feedstock, and to provide partially degraded organic material which functions as input to further processing steps and/or sequences.
  • a first material 2 that includes cellulose having a first number average molecular weight ( T M N1 ) and having a first oxygen content ( T O 1 ) is oxidized, e.g., by heating the first material in a tube furnace in stream of air or oxygen-enriched air, to provide a second material 3 that includes cellulose having a second number average molecular weight ( T M N2 ) and having a second oxygen content ( T O 2 ) higher than the first oxygen content ( T O 1 ).
  • the second material (or the first and second material in certain embodiments) can be, e.g., combined with a resin, such as a molten thermoplastic resin or a microorganism, to provide a composite 4 having desirable mechanical properties, or a fuel 5.
  • a resin such as a molten thermoplastic resin or a microorganism
  • Providing a higher level of oxidation can improve dispersability of the oxidized material in a resin and can also improve the interfacial bond between the oxidized material and the resin.
  • Improved dispersability and/or interfacial bonding (in some instances in combination with maintaining molecular weight) can provide composites with exceptional mechanical properties, such as improved abrasion resistance, compression strength, fracture resistance, impact strength, bending strength, tensile modulus, flexural modulus and elongation at break.
  • Such materials can also be combined with a solid and/or a liquid.
  • the liquid can be in the form of a solution and the solid can be particulate in form.
  • the liquid and/or solid can include a microorganism, e.g.; a bacterium, and/or an enzyme.
  • the bacterium and/or enzyme can work on the cellulosic or lignocellulosic material to produce a fuel, such as ethanol, or a coproduct, such as a protein.
  • Fuels and coproducts are described in FIBROUS MATERIALS AND COMPOSITES," USSN 11/453,951, filed June 15, 2006 .. The entire contents of each of the foregoing applications are incorporated herein by reference.
  • the starting number average molecular weight (prior to oxidation) is from about 200,000 to about 3,200,000, e.g., from about 250,000 to about 1,000,000 or from about 250,000 to about 700,000, and the number average molecular weight after oxidation is from about 175,000 to about 3,000,000, e.g., from about 200,000 to about 750,000 or from about 225,000 to about 600,000.
  • Resins utilized can be thermosets or thermoplastics.
  • thermoplastic resins include rigid and elastomeric thermoplastics.
  • Rigid thermoplastics include polyolefins (e.g., polyethylene, polypropylene, or polyolefin copolymers), polyesters (e.g., polyethylene terephthalate), polyamides (e.g., nylon 6,6/12 or 6/10), and polyethyleneimines.
  • elastomeric thermoplastic resins include elastomeric styrenic copolymers (e.g., styrene-ethylene-butylene-styrene copolymers), polyamide elastomers (e.g., polyether-polyamide copolymers) and ethylene-vinyl acetate copolymer.
  • elastomeric styrenic copolymers e.g., styrene-ethylene-butylene-styrene copolymers
  • polyamide elastomers e.g., polyether-polyamide copolymers
  • ethylene-vinyl acetate copolymer ethylene-vinyl acetate copolymer
  • lignin is utilized, e.g., any lignin that is generated in any process described herein.
  • the thermoplastic resin has a polydispersity index (PDI), i.e., a ratio of the weight average molecular weight to the number average molecular weight, of greater than 1.5, e.g., greater than 2.0, greater than 2.5, greater than 5.0, greater than 7.5, or even greater than 10.0.
  • PDI polydispersity index
  • polyolefins or blends of polyolefins are utilized as the thermoplastic resin.
  • thermosetting resins examples include natural rubber, butadiene-rubber and polyurethanes.
  • the starting number average molecular weight (prior to oxidation) is from about 200,000 to about 3,200,000, e.g., from about 250,000 to about 1,000,000 or from about 250,000 to about 700,000, and the number average molecular weight after oxidation is from about 50,000 to about 200,000, e.g., from about 60,000 to about 150,000 or from about 70,000 to about 125,000.
  • the number average molecular weight after extensive oxidation it is possible to have a number average molecular weight of less than about 10,000 or even less than about 5,000.
  • the second oxygen content is at least about five percent higher than the first oxygen content, e.g., 7.5 percent higher, 10.0 percent higher, 12.5 percent higher, 15.0 percent higher or 17.5 percent higher. In some preferred embodiments, the second oxygen content is at least about 20.0 percent higher than the oxygen content of the first material.
  • Oxygen content is measured by elemental analysis by pyrolyzing a sample in a furnace operating 1300 °C or higher.
  • a suitable elemental analyzer is the LECO CHNS-932 analyzer with a VTF-900 high temperature pyrolysis furnace.
  • oxidation of first material 200 does not result in a substantial change in the crystallinity of the cellulose.
  • the second material has cellulose that has as crystallinity ( T C 2 ) that is lower than the crystallinity ( T C 1 ) of the cellulose of the first material.
  • ( T C 2 ) can be lower than ( T C 1 ) by more than about 5 percent, e.g., 10, 15, 20, or even 25 percent.
  • This can be desirable when optimizing the flexural fatigue properties of the composite is a goal.
  • reducing the crystallinity can improve the elongation at break or can enhance the impact resistance of a composite.
  • This can also be desirable to enhance solubility of the materials in a liquid, such as a liquid that includes a bacterium and/or an enzyme.
  • the starting crystallinity index (prior to oxidation) is from about 40 to about 87.5 percent, e.g., from about 50 to about 75 percent or from about 60 to about 70 percent, and the crystallinity index after oxidation is from about 30 to about 75.0 percent, e.g., from about 35.0 to about 70.0 percent or from about 37.5 to about 65.0 percent.
  • the material after oxidation is substantially amorphous.
  • the resin can include a component that includes hydrogen-bonding groups, such as one or more anhydride groups, carboxylic acid groups, hydroxyl groups, amide groups, amine groups or mixtures of any of these groups.
  • the component includes a polymer copolymerized with and/or grafted with maleic anhydride. Such materials are available from Dupont under the tradename FUSABOND ® .
  • oxidation of first material 200 occurs in an oxidizing environment.
  • the oxidation can be effected or aided by pyrolysis in an oxidizing environment, such as in air or argon enriched in air.
  • various chemical agents such as oxidants, acids or bases can be added to the material prior to or during oxidation.
  • a peroxide e.g., benzoyl peroxide
  • benzoyl peroxide can be added prior to oxidation.
  • FIG. 22 shows a process flow diagram 5000 that includes various steps in an oxidative feedstock pretreatment system.
  • a supply of dry feedstock is received from a feed source.
  • the feed source can include, for example, a storage bed or container that is connected to an in-line oxidation reactor via a conveyor belt or another feedstock transport device.
  • the dry feedstock from the feed source may be pre-processed prior to delivery to the oxidation reactor.
  • the feedstock is derived from plant sources, certain portions of the plant material may be removed prior to collection of the plant material and/or before the plant material is delivered by the feedstock transport device.
  • the biomass feedstock can be subjected to mechanical processing (e.g., to reduce the average length of fibers in the feedstock) prior to delivery to the oxidation reactor.
  • feedstock 5030 is transported to a mixing system which introduces water 5150 into the feedstock in a mechanical mixing process. Combining water with the processed feedstock in mixing step 5040 creates an aqueous feedstock slurry 5050 which can then be treated with one or more oxidizing agents.
  • aqueous feedstock slurry 5050 includes from about 0.5 kg to about 1.0 kg of dry biomass per liter of water.
  • one or more fiber-protecting additives 5170 can also be added to the feedstock slurry in feedstock mixing step 5040.
  • Fiber-protecting additives help to reduce degradation of certain types of biomass fibers (e.g., cellulose fibers) during oxidation of the feedstock.
  • Fiber-protecting additives can be used, for example, if a desired product from processing a lignocellulosic feedstock includes cellulose fibers.
  • Exemplary fiber-protecting additives include magnesium compounds such as magnesium hydroxide. Concentrations of fiber-protecting additives in feedstock slurry 5050 can be from 0.1% to 0.4% of the dry weight of the biomass feedstock, for example.
  • aqueous feedstock slurry 5050 can be subjected to an optional extraction 5180 with an organic solvent to remove water-insoluble substances from the slurry.
  • extraction of slurry 5050 with one or more organic solvents yields a purified slurry and an organic waste stream 5210 that includes water-insoluble materials such as fats, oils, and other non-polar, hydrocarbon-based substances.
  • Suitable solvents for performing extraction of slurry 5050 include various alcohols, hydrocarbons, and halo-hydrocarbons, for example.
  • aqueous feedstock slurry 5050 can be subjected to an optional thermal treatment 5190 to further prepare the feedstock for oxidation.
  • An example of a thermal treatment includes heating the feedstock slurry in the presence of pressurized steam. In fibrous biomass feedstock, the pressurized steam swells the fibers, exposing a larger fraction of fiber surfaces to the aqueous solvent and to oxidizing agents that are introduced in subsequent processing steps.
  • aqueous feedstock slurry 5050 can be subjected to an optional treatment with basic agents 5200.
  • Treatment with one or more basic agents can help to separate lignin from cellulose in lignocellulosic biomass feedstock, thereby improving subsequent oxidation of the feedstock.
  • Exemplary basic agents include alkali and alkaline earth hydroxides such as sodium hydroxide, potassium hydroxide, and calcium hydroxide. In general, a variety of basic agents can be used, typically in concentrations from about 0.01% to about 0.5% of the dry weight of the feedstock.
  • Aqueous feedstock slurry 5050 is transported (e.g., by an in-line piping system) to a chamber, which can be an oxidation preprocessing chamber or an oxidation reactor.
  • oxidation preprocessing step 5060 one or more oxidizing agents 5160 are added to feedstock slurry 5050 to form an oxidizing medium.
  • oxidizing agents 5160 can include hydrogen peroxide. Hydrogen peroxide can be added to slurry 5050 as an aqueous solution, and in proportions ranging from 3% to between 30% and 35% by weight of slurry 5050.
  • Hydrogen peroxide has a number of advantages as an oxidizing agent
  • aqueous hydrogen peroxide solution is relatively inexpensive, is relatively chemically stable, is not particularly hazardous relative to other oxidizing agents (and therefore does not require burdensome handling procedures and expensive safety equipment).
  • hydrogen peroxide decomposes to form water during oxidation of feedstock, so that waste stream cleanup is relatively straightforward and inexpensive.
  • oxidizing agents 5160 can include oxygen (e.g., oxygen gas) either alone, or in combination with hydrogen peroxide.
  • oxygen gas can be bubbled into slurry 5050 in proportions ranging from 0.5% to 10% by weight of slurry 5050.
  • oxygen gas can also be introduced into a gaseous phase in equilibrium with slurry 5050 (e.g., a vapor head above slurry 5050).
  • the oxygen gas can be introduced into either an oxidation preprocessing chamber or into an oxidation reactor (or into both), depending upon the configuration of the oxidative processing system.
  • the partial pressure of oxygen in the vapor above slurry 5050 is larger than the ambient pressure of oxygen, and ranges from 0.5 bar to 35 bar, depending upon the nature of the feedstock.
  • the oxygen gas can be introduced in pure form, or can be mixed with one or more carrier gases.
  • high-pressure air provides the oxygen in the vapor.
  • oxygen gas can be supplied continuously to the vapor phase to ensure that a concentration of oxygen in the vapor remains within certain predetermined limits during processing of the feedstock.
  • oxygen gas can be introduced initially in sufficient concentration to oxidize the feedstock, and then the feedstock can be transported to a closed, pressurized vessel (e.g., an oxidation reactor) for processing.
  • oxidizing agents 5160 can include nascent oxygen (e.g., oxygen radicals).
  • nascent oxygen is produced as needed in an oxidation reactor or in a chamber in fluid communication with an oxidation reactor by one or more decomposition reactions.
  • nascent oxygen can be produced from a reaction between NO and O 2 in a gas mixture or in solution.
  • nascent oxygen can be produced from decomposition of HOCl in solution.
  • Other methods by which nascent oxygen can be produced include via electrochemical generation in electrolyte solution, for example.
  • nascent oxygen is an efficient oxidizing agent due to the relatively high reactivity of the oxygen radical.
  • nascent oxygen can also be a relatively selective oxidizing agent.
  • oxidation of feedstock with nascent oxygen provides a method for selective removal of the lignin fraction in certain feedstocks.
  • nascent oxygen concentrations of between about 0.5% and 5% of the dry weight of the feedstock are used to effect efficient oxidation.
  • nascent oxygen reacts with lignocellulosic feedstock according to at least two different mechanisms.
  • nascent oxygen undergoes an addition reaction with the lignin, resulting in partial oxidation of the lignin, which solubilizes the lignin in aqueous solution.
  • the solubilized lignin can be removed from the rest of the feedstock via washing.
  • nascent oxygen disrupts butane cross-links and/or opens aromatic rings that are connected via the butane cross-links.
  • solubility of the lignin in aqueous solution increases, and the lignin fraction can be separated from the remainder of the feedstock via washing.
  • oxidizing agents 5160 include ozone (O 3 ).
  • O 3 ozone
  • the use of ozone can introduce several chemical handling considerations in the oxidation processing sequence. If heated too vigorously, an aqueous solution of ozone can decompose violently, with potentially adverse consequences for both human system operators and system equipment. Accordingly, ozone is typically generated in a thermally isolated, thick-walled vessel separate from the vessel that contains the feedstock slurry, and transported thereto at the appropriate process stage.
  • Ozone decomposes into oxygen and oxygen radicals, and that the oxygen radicals (e.g., nascent oxygen) are responsible for the oxidizing properties of ozone in the manner discussed above.
  • Ozone typically preferentially oxidizes the lignin fraction in lignocellulosic materials, leaving the cellulose fraction relatively undisturbed.
  • Conditions for ozone-based oxidation of biomass feedstock generally depend upon the nature of the biomass. For example, for cellulosic and/or lignocellulosic feedstocks, ozone concentrations of from 0.1 g/m 3 to 20 g/m 3 of dry feedstock provide for efficient feedstock oxidation.
  • the water content in slurry 5050 is between 10% by weight and 80% by weight (e.g., between 40% by weight and 60% by weight).
  • the temperature of slurry 5050 can be maintained between 0°C and 100 °C to avoid violent decomposition of the ozone.
  • feedstock slurry 5050 can be treated with an aqueous, alkaline solution that includes one or more alkali and alkaline earth hydroxides such as sodium hydroxide, potassium hydroxide, and calcium hydroxide, and then treated thereafter with an ozone-containing gas in an oxidation reactor.
  • This process has been observed to significantly increase decomposition of the biomass in slurry 5050.
  • a concentration of hydroxide ions in the alkaline solution is between 0.001% and 10% by weight of slurry 5050.
  • the ozone-containing gas is introduced into the oxidation reactor, where it contacts and oxidizes the feedstock.
  • Oxidizing agents 5160 can also include other substances.
  • halogen-based oxidizing agents such as chlorine and oxychlorine agents (e.g., hypochlorite) can be introduced into slurry 5050.
  • nitrogen-containing oxidizing substances can be introduced into slurry 5050.
  • Exemplary nitrogen-containing oxidizing substances include NO and NO 2 , for example.
  • Nitrogen-containing agents can also be combined with oxygen in slurry 5050 to create additional oxidizing agents. For example, NO and NO 2 both combine with oxygen in slurry 5050 to form nitrate compounds, which are effective oxidizing agents for biomass feedstock.
  • Halogen- and nitrogen-based oxidizing agents can, in some embodiments, cause bleaching of the biomass feedstock, depending upon the nature of the feedstock. The bleaching may be desirable for certain biomass-derived products that are extracted in subsequent processing steps.
  • oxidizing agents can include, for example, various peroxyacids, peroxyacetic acids, persulfates, percarbonates, permanganates, osmium tetroxide, and chromium oxides.
  • feedstock slurry 5050 is oxidized in step 5070. If oxidizing agents 5160 were added to slurry 5050 in an oxidation reactor, then oxidation proceeds in the same reactor. Alternatively, if oxidizing agents 5160 were added to slurry 5050 in a preprocessing chamber, then slurry 5050 is transported to an oxidation reactor via an in-line piping system. Once inside the oxidation reactor, oxidation of the biomass feedstock proceeds under a controlled set of environmental conditions. Typically, for example, the oxidation reactor is a cylindrical vessel that is closed to the external environment and pressurized. Both batch and continuous operation is possible, although environmental conditions are typically easier to control in in-line batch processing operations.
  • Oxidation of feedstock slurry 5050 typically occurs at elevated temperatures in the oxidation reactor.
  • the temperature of slurry 5050 in the oxidation reactor is typically maintained above 100°C, in a range from 120°C to 240°C.
  • oxidation is particularly efficient if the temperature of slurry 5050 is maintained between 150°C and 220 °C.
  • Slurry 5050 can be heating using a variety of thermal transfer devices.
  • the oxidation reactor contacts a heating bath that includes oil or molten salts.
  • a series of heat exchange pipes surround and contact the oxidation reactor, and circulation of hot fluid within the pipes heats slurry 5050 in the reactor.
  • Other heating devices that can be used to heat slurry 5050 include resistive heating elements, induction heaters, and microwave sources, for example.
  • the residence time of feedstock slurry 5050 in the oxidation reactor can be varied as desired to process the feedstock. Typically, slurry 5050 spends from 1 minute to 60 minutes undergoing oxidation in the reactor. For relatively soft biomass material such as lignocellulosic matter, the residence time in the oxidation reactor can be from 5 minutes to 30 minutes, for example, at an oxygen pressure of between 3 and 12 bars in the reactor, and at a slurry temperature of between 160°C and 210 °C. For other types of feedstock, however, residence times in the oxidation reactor can be longer, e.g., as long 48 hours.
  • aliquots of the slurry can be extracted from the reactor at specific intervals and analyzed to determine concentrations of particular products of interest such as complex saccharides.
  • Information about the increase in concentrations of certain products in slurry 5050 as a function of time can be used to determine residence times for particular classes of feedstock material.
  • adjustment of the slurry pH may be performed by introducing one or more chemical agents into the oxidation reactor.
  • oxidation occurs most efficiently in a pH range of about 9-11.
  • agents such as alkali and alkaline earth hydroxides, carbonates, ammonia, and alkaline buffer solutions can be introduced into the oxidation reactor.
  • Circulation of slurry 5050 during oxidation can be important to ensure sufficient contact between oxidizing agents 5160 and the feedstock. Circulation of the slurry can be achieved using a variety of techniques. For example, in some embodiments, a mechanical stirring apparatus that includes impeller blades or a paddle wheel can be implemented in the oxidation reactor. In certain embodiments, the oxidation reactor can be a loop reactor, in which the aqueous solvent in which the feedstock is suspended is simultaneously drained from the bottom of the reactor and recirculated into the top of the reactor via pumping, thereby ensuring that the slurry is continually re-mixed and does not stagnate within the reactor.
  • mechanical separation step 5080 includes one or more stages of increasingly-fine filtering of the slurry to mechanically separate the solid and liquid constituents.
  • Liquid phase 5090 is separated from solid phase 5100, and the two phases are processed independently thereafter.
  • Solid phase 5100 can optionally undergo a drying step 5120 in a drying apparatus, for example. Drying step 5120 can include, for example, mechanically dispersing the solid material onto a drying surface, and evaporating water from solid phase 5100 by gentle heating of the solid material. Following drying step 5120 (or, alternatively, without undergoing drying step 5120), solid phase 5100 is transported for further processing steps 5140.
  • Liquid phase 5090 can optionally undergo a drying step 5110 to reduce the concentration of water in the liquid phase.
  • drying step 5110 can include evaporation and/or distillation and/or extraction of water from liquid phase 5090 by gentle heating of the liquid.
  • one or more chemical drying agents can be used to remove water from liquid phase 5090.
  • liquid phase 5090 is transported for further processing steps 5130, which can include a variety of chemical and biological treatment steps such as chemical and/or enzymatic hydrolysis.
  • Drying step 5110 creates waste stream 5220, an aqueous solution that can include dissolved chemical agents such as acids and bases in relatively low concentrations.
  • Treatment of waste stream 5220 can include, for example, pH neutralization with one or more mineral acids or bases.
  • the solution may be partially de-ionized (e.g., by passing the waste stream through an ion exchange system). Then, the waste stream - which includes primarily water - can be re-circulated into the overall process (e.g., as water 5150), diverted to another process, or discharged.
  • liquid phase 5090 typically includes a variety of soluble poly- and oligosaccharides, which can then be separated and/or reduced to smaller-chain saccharides via further processing steps.
  • Solid phase 5100 typically includes primarily cellulose, for example, with smaller amounts of hemicellulose- and lignin-derived products.
  • oxidation can be carried out at elevated temperature in a reactor such as a pyrolysis chamber.
  • feedstock materials can be oxidized in filament pyrolyzer 1712.
  • an oxidizing carrier gas e.g., air or an air/argon blend
  • a desired temperature e.g., 325 °C.
  • an appropriate time e.g., 5 to 10 minutes
  • the oxidized material is emptied from the sample holder.
  • the system shown in FIG. 2 can be scaled and made continuous.
  • the heating member can be an auger screw. Material can continuously fall into the sample holder, striking a heated screw that pyrolizes the material. At the same time, the screw can push the oxidized material out of the sample holder to allow for the entry of fresh, unoxidized material.
  • feedstock materials can be oxidized in a Curie-Point pyrolyzer 1820.
  • an oxidizing carrier gas traverses through the sample chamber 1821 while the foil 1822 is inductively heated by an applied RF field to oxidize the material at a desired temperature.
  • feedstock materials can be oxidized in a furnace pyrolyzer 130.
  • the sample is lowered (as indicated by arrow 137) into a hot zone 135 of furnace 132, while an oxidizing carrier gas fills the housing 136 and traverses through the sample holder 131.
  • the sample is heated to the desired temperature for a desired time to provide an oxidized product.
  • the oxidized product is removed from the pyrolyzer by raising the sample holder (as indicated by arrow 134).
  • feedstock materials can be oxidized by forming a cellulosic target 140, along with an oxidant, such as a peroxide, and treating the target, which is housed in a vacuum chamber 141, with laser light, e.g., light having a wavelength of from about 225 nm to about 1600 nm.
  • laser light e.g., light having a wavelength of from about 225 nm to about 1600 nm.
  • the optical configuration shown allows the monochromatic light 143 generated by the laser 142 to be directed using mirrors 144 and 145 onto the target after passing though a lens 146 in the vacuum chamber 141.
  • the pressure in the vacuum chamber is maintained at less than about 10 -6 mm Hg.
  • infrared radiation is used, e.g., 1.06 micron radiation from a Nd-YAG laser.
  • a infrared sensitive dye can be combined with the cellulosic material to produce a cellulosic target.
  • the infrared dye can enhance the heating of the cellulosic material.
  • Laser treatment of polymers is described by Blanchet-Fincher et al. in U.S. Patent No. 5,942,649 .
  • feedstock materials can be rapidly oxidized by coating a tungsten filament 150, together with an oxidant, such as a peroxide, with the desired cellulosic material while the material is housed in a vacuum chamber 151.
  • an oxidant such as a peroxide
  • current is passed through the filament, which causes a rapid heating of the filament for a desired time.
  • the heating is continued for seconds before allowing the filament to cool.
  • the heating is performed a number of times to effect the desired amount of oxidation.
  • feedstock materials can be oxidized with the aid of sound and/or cavitation.
  • the materials are sonicated in an oxidizing environment, such as water saturated with oxygen or another chemical oxidant, such as hydrogen peroxide.
  • ionizing radiation is used to aid in the oxidation of feedstock materials.
  • the materials are irradiated in an oxidizing environment, such as air or oxygen.
  • gamma radiation and/or electron beam radiation can be employed to irradiate the materials.
  • FIG 23 shows an overview of the entire process of converting a fiber source 400 into a product 450, such as ethanol, by a process that includes shearing and steam explosion to produce a fibrous material 401, which is then hydrolyzed and converted, e.g., fermented, to produce the product.
  • the fiber source can be transformed into the fibrous material 401 through a number of possible methods, including at least one shearing process and at least one steam explosion process.
  • one option includes shearing the fiber source, followed by optional screening step(s) and optional additional shearing step(s) to produce a sheared fiber source 402, which can then be steam exploded to produce the fibrous material 401.
  • the steam explosion process is optionally followed by a fiber recovery process to remove liquids or the "liquor" 404, resulting from the steam exploding process.
  • the material resulting from steam exploding the sheared fiber source may be further sheared by optional additional shearing step(s) and/or optional screening step(s).
  • the fibrous material 401 is first steam exploded to produce a steam exploded fiber source 410.
  • the resulting steam exploded fiber source is then subjected to an optional fiber recovery process to remove liquids, or the liquor.
  • the resulting steam exploded fiber source can then be sheared to produce the fibrous material.
  • the steam exploded fiber source can also be subject to one or more optional screening steps and/or one or more optional additional shearing steps. The process of shearing and steam exploding the fiber source to produce the sheared and steam exploded fibrous material will be further discussed below.
  • the fiber source can be cut into pieces or strips of confetti material prior to shearing or steam explosion.
  • the shearing processes can take place in a dry (e.g., having less than 0.25 percent by weight absorbed water), hydrated, or even while the material is partially or fully submerged in a liquid, such as water or isopropanol.
  • the process can also optimally include steps of drying the output after steam exploding or shearing to allow for additional steps of dry shearing or steam exploding.
  • the steps of shearing, screening, and steam explosion can take place with or without the presence of various chemical solutions.
  • the fiber source or the sheared fiber source is contacted with steam under high pressure, and the steam diffuses into the structures of the fiber source (e.g., the lignocellulosic structures).
  • the steam then condenses under high pressure thereby "wetting" the fiber source.
  • the moisture in the fiber source can hydrolyze any acetyl groups in the fiber source (e.g., the acetyl groups in the hemicellulose fractions), forming organic acids such as acetic and uronic acids.
  • the acids in turn, can catalyze the depolymerization of hemicellulose, releasing xylan and limited amounts of glucan.
  • the "wet” fiber source (or sheared fiber source, etc.) is then "exploded” when the pressure is released.
  • the condensed moisture instantaneously evaporates due to the sudden decrease in pressure and the expansion of the water vapor exerts a shear force upon the fiber source (or sheared fiber source, etc.).
  • a sufficient shear force will cause the mechanical breakdown of the internal structures (e.g., the the ligocellulosic struructures) of the fiber source.
  • the sheared and steam exploded fibrous material is then converted into a useful product, such as ethanol.
  • the fibrous material is converted into a fuel.
  • One method of converting the fibrous material into a fuel is by hydrolysis to produce fermentable sugars, 412, which are then fermented to produce the product.
  • Other known and unknown methods of converting fibrous materials into fuels may also be used.
  • the sheared and steam exploded fibrous material 401 is sterilized to kill any competing microorganisms that may be on the fibrous material.
  • the fibrous material can be sterilized by exposing the fibrous material to radiation, such as infrared radiation, ultraviolet radiation, or an ionizing radiation, such as gamma radiation.
  • the microorganisms can also be killed using chemical sterilants, such as bleach (e.g., sodium hypochlorite), chlorhexidine, or ethylene oxide.
  • Cellulases are a group of enzymes that act synergistically to hydrolyze cellulose.
  • AccelleraseTM 1000 which contains a complex of enzymes that reduces lignocellulosic biomass into fermentable sugars can also be used.
  • cellulase include endoglucanases, exoglucanases (cellobiohydrolases), and b-glucosidases (cellobiases). Synergism between the cellulase components exists when hydrolysis by a combination of two or more components exceeds the sum of the activities expressed by the individual components.
  • the generally accepted mechanism of a cellulase system (particularly of T. longibrachiatum ) on crystalline cellulose is: endoglucanase hydrolyzes internal ⁇ -1,4-glycosidic bonds of the amorphous regions, thereby increasing the number of exposed non-reducing ends.
  • Exoglucanases then cleave off cellobiose units from the nonreducing ends, which in turn are hydrolyzed to individual glucose units by b-gluocosidases.
  • the synergistic action of the components in various configurations is required for optimum cellulose hydrolysis.
  • Cellulases are more inclined to hydrolyze the amorphous regions of cellulose.
  • a linear relationship between crystallinity and hydrolysis rates exists whereby higher crystallinity indices correspond to slower enzyme hydrolysis rates.
  • Amorphous regions of cellulose hydrolyze at twice the rate of crystalline regions.
  • the hydrolysis of the sheared and steam exploded fibrous material may be performed by any hydrolyzing biomass process.
  • the process of converting the sheared and steam exploded fibrous material into a fuel can therefore optionally include an overliming step prior to fermentation to precipitate some of the toxicants.
  • the pH of the sheared and steam exploded fibrous material may be raised to exceed the pH of 10 by adding calcium hydroxide (Ca(OH) 2 ) followed by a step of lowering the pH to about 5 by adding H 2 SO 4 .
  • the overlimed fibrous material may then be used as is without the removal of precipitates.
  • the optional overliming step occurs just prior to the step of hydrolysis of the sheared and steam exploded fibrous material, but it is also contemplated to perform the overliming step after the hydrolysis step and prior to the fermenting step.
  • FIG. 24 depicts an example of a steam explosion apparatus 460.
  • the steam explosion apparatus 460 includes a reaction chamber 462, in which the fiber source and/or the fibrous material placed through a fiber source inlet 464.
  • the reaction chamber is sealed by closing fiber source inlet valve 465.
  • the reaction chamber further includes a pressurized steam inlet 466 that includes a steam valve 467.
  • the reaction chamber further includes an explosive depressurization outlet 468 that includes an outlet valve 469 in communication with the cyclone 470 through the connecting pipe 472.
  • the holding time begins.
  • the reaction temperature is held at the target temperature for the desired holding time, which typically lasts from about 10 seconds to 5 minutes.
  • outlet valve is open to allow for explosive depressurization to occur.
  • the process of explosive depressurization propels the contents of the reaction chamber 462 out of the explosive depressurization outlet 468, through the connecting pipe 472, and into the cyclone 470.
  • the steam exploded fiber source or fibrous material then exits the cyclone in a sludge form into the collection bin 474 as much of the remaining steam exits the cyclone into the atmosphere through vent 476.
  • the steam explosion apparatus further includes wash outlet 478 with wash outlet valve 479 in communication with connecting pipe 472.
  • the wash outlet valve 479 is closed during the use of the steam explosion apparatus 460 for steam explosion, but opened during the washing of the reaction chamber 462.
  • the target temperature of the reaction chamber 462 is preferably between 180 and 240 degrees Celsius or between 200 and 220 degrees Celsius.
  • the holding time is preferably between 10 seconds and 30 minutes, or between 30 seconds and 10 minutes, or between 1 minute and 5 minutes.
  • the steam exploded fibrous material may optionally include a fiber recovery process where the "liquor" is separated from the steam exploded fibrous material.
  • This fiber recovery step is helpful in that it enables further shearing and/or screening processes and can allow for the conversion of the fibrous material into fuel.
  • the fiber recovery process occurs through the use of a mesh cloth to separate the fibers from the liquor. Further drying processes can also be included to prepare the fibrous material or steam exploded fiber source for subsequent processing.
  • Any processing technique described herein can be used at pressure above or below normal, earth-bound atmospheric pressure.
  • any process that utilizes radiation, sonication, oxidation, pyrolysis, steam explosion, or combinations of any of these processes to provide materials that include a carbohydrate can be performed under high pressure, which, can increase reaction rates.
  • any process or combination of processes can be performed at a pressure greater than about greater than 25 MPa, e.g., greater than 50 MPa, 75 MPa, 100 MPa, 150 MPa, 200 MPa, 250 MPa, 350 MPa, 500 MPa, 750 MPa, 1,000 MPa, or greater than 1,500 MPa.
  • multiple processes may be performed in close juxtaposition or even simultaneously, with the benefit of increasing pretreatment throughput and potential cost savings.
  • each separate process is effective in lowering the mean molecular weight of cellulosic material by an order of magnitude or more, and by several orders of magnitude when performed serially.
  • Hybrid electron beam/sonication device 2500 is pictured above a shallow pool (depth - 3-5 cm) of a slurry of cellulosic material 2550 dispersed in an aqueous, oxidant medium, such as hydrogen peroxide or carbamide peroxide.
  • Hybrid device 2500 has an energy source 2510, which powers both electron beam emitter 2540 and sonication horns 2530..
  • Electron beam emitter 2540 generates electron beams which pass though an electron beam aiming device 2545 to impact the slurry 2550 containing cellulosic material.
  • the electron beam aiming device can be a scanner that sweeps a beam over a range of up to about 6 feet in a direction approximately parallel to the surface of the slurry 2550.
  • sonication horns 2530 On either side of the electron beam emitter 2540 are sonication horns 2530, which deliver ultrasonic wave energy to the slurry 2550.
  • the sonication horns 2530 end in a detachable endpiece 2535 that is in contact with the slurry 2550.
  • the sonication horns 2530 are at risk of damage from long-term residual exposure to the electron beam radiation.
  • the horns can be protected with a standard shield 2520, e.g., made of lead or a heavy-metal-containing alloy such as Lipowitz metal, which is impervious to electron beam radiation. Precautions must be taken, however, to ensure that the ultrasonic energy is not affected by the presence of the shield.
  • the detachable endpieces 2535 are constructed of the same material and attached to the horns 2530, are used to be in contact with the cellulosic material 2550 and are expected to be damaged. Accordingly, the detachable endpieces 2535 are constructed to be easily replaceable.
  • a further benefit of such a simultaneous electron beam and ultrasound process is that the two processes have complementary results.
  • electron beam irradiation alone an insufficient dose may result in cross-linking of some of the polymers in the cellulosic material, which lowers the efficiency of the overall depolymerization process.
  • Lower doses of electron beam irradiation and/or ultrasound radiation may also be used to achieve a similar degree of depolymerization as that achieved using electron beam irradiation and sonication separately.
  • An electron beam device can also be combined with one or more of high-frequency, rotor-stator devices, which can be used as an alternative to ultrasonic energy devices, and performs a similar function.
  • an ionizing radiation device that produces gamma radiation emitted from, e.g., 60 Co pellets, can be combined with an electron beam source and/or an ultrasonic wave source. Shielding requirements may be more stringent in this case.
  • the radiation devices for pretreating biomass discussed above can also be combined with one or more devices that perform one or more pyrolysis processing sequences. Such a combination may again have the advantage of higher throughput. Nevertheless, caution must be observed, as there may be conflicting requirements between some radiation processes and pyrolysis. For example, ultrasonic radiation devices may require the feedstock be immersed in a liquid oxidizing medium. On the other hand, as discussed previously, it may be advantageous for a sample of feedstock undergoing pyrolysis to be of a particular moisture content. In this case, the new systems automatically measure and monitor for a particular moisture content and regulate the same Further, some or all of the above devices, especially the pyrolysis device, can be combined with an oxidation device as discussed previously.
  • various microorganisms can produce a number of useful products, such as a fuel, by operating on, e.g., fermenting the pretreated biomass materials.
  • useful products such as a fuel
  • fermenting the pretreated biomass materials For example, alcohols, organic acids, hydrocarbons, hydrogen, proteins or mixtures of any of these materials can be produced by fermentation or other processes.
  • the microorganism can be a natural microorganism or an engineered microorganism.
  • the microorganism can be a bacterium, e.g., a cellulolytic bacterium, a fungus, e.g., a yeast, a plant or a protist, e.g., an algae, a protozoa or a fungus-like protist, e.g., a slime mold.
  • a bacterium e.g., a cellulolytic bacterium
  • a fungus e.g., a yeast
  • a protist e.g., an algae, a protozoa or a fungus-like protist, e.g., a slime mold.
  • mixtures of organisms can be utilized.
  • one or more enzymes e.g., a cellulolytic enzyme can be utilized.
  • the materials that include the cellulose are first treated with the enzyme, e.g., by combining the material and the enzyme in an aqueous solution. This material can then be combined with the microorganism.
  • the materials that include the cellulose, the one or more enzymes and the microorganism are combined at the concurrently, e.g., by combining in an aqueous solution.
  • the materials can be treated post irradiation with heat, a chemical (e.g., mineral acid, base or a strong oxidizer such as sodium hypochlorite), and/or an enzyme.
  • a chemical e.g., mineral acid, base or a strong oxidizer such as sodium hypochlorite
  • sugars released from cellulolytic hydrolysis or the saccharification step are fermented to, e.g., ethanol, by a fermenting microorganism such as yeast.
  • a fermenting microorganism such as yeast.
  • Suitable fermenting microorganisms have the ability to convert carbohydrates, such as glucose, xylose, arabinose, mannose, galactose, oligosaccharides or polysaccharides into fermentation products.
  • Fermenting microorganisms include strains of the genus Sacchromyces spp.
  • Sacchromyces cerevisiae (baker's yeast), Saccharomyces distaticus, Saccharomyces uvarum; the genus Kluyveromyces, e.g., species Kluyveromyces marxianus, Kluyveromyces fragilis; the genus Candida, e.g., Candida pseudotropicalis, and Candida brassicae, the genus Clavispora, e.g., species Clavispora lusitaniae and Clavispora opuntiae the genus Pachysolen, e.g., species Pachysolen tannophilus, the genus Bretannomyces, e.g., species Bretannomyces clausenii ( Philippidis, G. P.,1996, Cellulose bioconversion technology, in Handbook on Bioethanol: Production and Utilization, Wyman, C.E., ed., Taylor & Francis, Washington, DC, 179-212 ).
  • yeast Commercially available yeast include, for example, Red Star®/Lesaffre Ethanol Red (available from Red Star/Lesaffre, USA) FALI ® (available from Fleischmann's Yeast, a division of Bums Philip Food Inc., USA), SUPERSTART ® (available from Alltech), GERT STRAND ® (available from Gert Strand AB, Sweden) and FERMOL ® (available from DSM Specialties).
  • Red Star®/Lesaffre Ethanol Red available from Red Star/Lesaffre, USA
  • FALI ® available from Fleischmann's Yeast, a division of Bums Philip Food Inc., USA
  • SUPERSTART ® available from Alltech
  • GERT STRAND ® available from Gert Strand AB, Sweden
  • FERMOL ® available from DSM Specialties.
  • Bacteria that can ferment bimoss to ethanol and other products include, e.g., Zymomonas mobilis and Clostridium thermocellum (Philippidis, 1996, supra). Leschine et al. (International Journal of Systematic and Evolutionary Mlcrobiology 2002, 52,1155-1160 ) isolated an anaerobic, mesophilic, cellulolytic bacterium from forest soil, Clostridium phytofermentans sp. nov., which converts cellulose to ethanol.
  • Fermentation of biomass to ethanol and other products may be carried out using certain types of thermophilic or genetically engineered microorganisms, such Thermoanaerobacter species, including T. mathranii, and yeast species such as Pichia species.
  • Thermoanaerobacter species including T. mathranii, and yeast species such as Pichia species.
  • T. mathranii An example of a strain of T. mathranii is A3M4 described in Sonne-Hansen et al. (Applied Microbiology and Biotechnology 1993, 38, 537-541 ) or Ahring et al. (Arch. Microbiol. 1997, 168, 114-119 ).
  • Yeast and Zymomonas bacteria can be used for fermentation or conversion.
  • the optimum pH for yeast is from about pH 4 to 5, while the optimum pH for Zymomonas is from about pH 5 to 6.
  • Typical fermentation times are about 24 to 96 hours with temperatures in the range of 26 °C to 40 °C, however thermophilic microorganisms prefer higher temperatures.
  • Enzymes which break down biomass, such as cellulose, to lower molecular weight carbohydrate-containing materials, such as glucose, during saccharification are referred to as cellulolytic enzymes or cellulase. These enzymes may be a complex of enzymes that act synergistically to degrade crystalline cellulose. Examples of cellulolytic enzymes include: endoglucanases, cellobiohydrolases, and cellobiases ( ⁇ -glucosidases). A cellulosic substrate is initially hydrolyzed by endoglucanases at random locations producing oligomeric intermediates.
  • cellobiose is a water-soluble ⁇ -1,4-linked dimer of glucose.
  • cellobiase cleaves cellobiose to yield glucose.
  • a cellulase is capable of degrading biomass and may be of fungal or bacterial origin.
  • Suitable enzymes include cellulases from the genera Bacillus, Pseudomonas, Humicola, Fusarium, Thielavia, Acremonium, Chrysosporium and Trichoderma, and include species of Humicola, Coprinus, Thielavia, Fusarium, Myceliophthora, Acremonium, Cephalosporium, Scytalidium, Penicillium or Aspergillus (see, e.g., EP 458162 ), especially those produced by a strain selected from the species Humicola insolens (reclassified as Scytalidium thermophilum, see, e.g., U.S.
  • Patent No. 4,435,307 Coprinus cinereus, Fusarium oxysporum, Myceliophthora thermophila, Meripilus giganteus, Thielavia terrestris, Acremonium sp., Acremonium persicinum, Acremonium acremonium, Acremonium brachypenium, Acremonium dichromosporum, Acremonium obclavatum, Acremonium pinkertoniae, Acremonium roseogriseum, Acremonium incoloratum, and Acremonium furatum; preferably from the species Humicola insolens DSM 1800, Fusarium axysporum DSM 2672, Myceliophthora thermophila CBS 117.65, Cephalosporium sp.
  • Cellulolytic enzymes may also be obtained from Chrysosporium, preferably a strain of Chrysosporium lucknowense. Additionally, Trichoderma (particularly Trichoderma viride, Trichoderma reesei, and Trichoderma koningii ), alkalophilic Bacillus (see, for example, U.S. Patent No. 3,844,890 and EP 458162 ), and Streptomyces (see, e.g., EP 458162 ) may be used.
  • Anaerobic cellulolytic bacteria have also been isolated from soil, e.g., a novel cellulolytic species of Clostiridium, Clostridium phytofermentans sp. nov. (see Leschine et. al, International Journal of Systematic and Evolutionary Microbiology (2002), 52, 1155-1160 ).
  • Cellulolytic enzymes using recombinant technology can also be used (see, e.g., WO 2007/071818 and WO 2006/110891 ).
  • the cellulolytic enzymes used can be produced by fermentation of the above-noted microbial strains on a nutrient medium containing suitable carbon and nitrogen sources and inorganic salts, using procedures known in the art (see, e.g., Bennett, J.W. and LaSure, L. (eds.), More Gene Manipulations in Fungi, Academic Press, CA 1991 ). Suitable media are available from commercial suppliers or may be prepared according to published compositions (e.g., in catalogues of the American Type Culture Collection).
  • Temperature ranges and other conditions suitable for growth and cellulase production are known in the art (see, e.g., Bailey, J.E., and Ollis, D.F., Biochemical Engineering Fundamentals, McGraw-Hill Book Company, NY,1986 ).
  • Treatment of cellulose with cellulase is usually carried out at temperatures between 30 °C and 65°C.
  • Cellulases are active over a range of pH of about 3 to 7.
  • a saccharification step may last up to 120 hours.
  • the cellulase enzyme dosage achieves a sufficiently high level of cellulose conversion.
  • an appropriate cellulase dosage is typically between 5.0 and 50 Filter Paper Units (FPU or IU) per gram of cellulose.
  • the FPU is a standard measurement and is defined and measured according to Ghose ( 1987, Pure and Appl. Chem. 59:257-268 ).
  • pyrolysis can also be used to process pre-treated feedstock to extract useful materials.
  • a form of pyrolysis known as gasification can be employed to generate fuel gases along with various other gaseous, liquid, and solid products.
  • gasification a form of pyrolysis known as gasification can be employed to generate fuel gases along with various other gaseous, liquid, and solid products.
  • the pre-treated feedstock is introduced into a pyrolysis chamber and heated to a high temperature, typically 700 °C or more. The temperature used depends upon a number of factors, including the nature of the feedstock and the desired products.
  • Quantities of oxygen e.g., as pure oxygen gas and/or as air
  • steam e.g., superheated steam
  • synthesis gas or "syngas”
  • a limited amount of oxygen is introduced into the pyrolysis chamber to allow some feedstock material to combust to form carbon monoxide and generate process heat. The process heat can then be used to promote a second reaction that converts additional feedstock material to hydrogen and carbon monoxide.
  • a first step of the overall reaction heating the feedstock material produces a char that can include a wide variety of different hydrocarbon-based species.
  • Certain volatile materials can be produced (e.g., certain gaseous hydrocarbon materials), resulting in a reduction of the overall weight of the feedstock material.
  • some of the volatile material that is produced in the first step reacts with oxygen in a combustion reaction to produce both carbon monoxide and carbon dioxide.
  • the combustion reaction releases heat, which promotes the third step of the reaction.
  • carbon dioxide and steam e.g., water
  • Carbon monoxide can also react with steam, in a water gas shift reaction, to form carbon dioxide and further hydrogen gas.
  • Gasification can be used as a primary process to generate products directly from pretreated feedstock for subsequent transport and/or sale, for example.
  • gasification can be used as an auxiliary process for generating fuel for an overall processing system.
  • the hydrogen-rich syngas that is generated via the gasification process can be burned, for example, to generate electricity and/or process heat that can be directed for use at other locations in the processing system.
  • the overall processing system can be at least partially self-sustaining.
  • a number of other products, including pyrolysis oils and gaseous hydrocarbon-based substances, can also be obtained during and/or following gasification; these can be separated and stored or transported as desired.
  • a variety of different pyrolysis chambers are suitable for gasification of pro-treated feedstock, including the pyrolysis chambers disclosed herein.
  • fluidized bed reactor systems in which the pre-treated feedstock is fluidized in steam and oxygen/air, provide relatively high throughput and straightforward recovery of products. Solid char that remains following gasification in a fluidized bed system (or in other pyrolysis chambers) can be burned to generate additional process heat to promote subsequent gasification reactions.
  • the resulting fluids can be distilled using, for example, a "beer column” to separate ethanol and other alcohols from the majority of water and residual solids.
  • the vapor exiting the beer column can be 35% by weight ethanol and fed to a rectification column.
  • a mixture of nearly azeotropic (92.5%) ethanol and water from the rectification column can be purified to pure (99.5%) ethanol using vapor-phase molecular sieves.
  • the beer column bottoms can be sent to the first effect of a three-effect evaporator.
  • the rectification column reflux condenser can provide heat for this first effect. After the first effect, solids can be separated using a centrifuge and dried in a rotary dryer.
  • a portion (25%) of the centrifuge effluent can be recycled to fermentation and the rest sent to the second and third evaporator effects. Most of the evaporator condensate can be returned to the process as fairly clean condensate with a small portion split off to waste water treatment to prevent build-up of low-boiling compounds.
  • Wastewater treatment is used to minimize makeup water requirements of the plant by treating process water for reuse within the plant. Wastewater treatment can also produce fuel (e.g., sludge and biogas) that can be used to improve the overall efficiency of the ethanol production process. For example, as described in further detail below, sludge and biogas can be used to create steam and electricity that can be used in various plant processes.
  • fuel e.g., sludge and biogas
  • sludge and biogas can be used to create steam and electricity that can be used in various plant processes.
  • Wastewater is initially pumped through a screen (e.g., a bar screen) to remove large particles, which are collected in a hopper.
  • a screen e.g., a bar screen
  • the large particles are sent to a landfill. Additionally or alternatively, the large particles are burned to create steam and/or electricity as described in further detail below.
  • the spacing on the bar screen is between 1/4 inch to 1 inch spacing (e.g.,1/2 inch spacing).
  • the wastewater then flows to an equalization tank, where the organic concentration of the wastewater is equalized during a retention time.
  • the retention time is between 8 hours and 36 hours (e.g., 24 hours).
  • a mixer is disposed within the tank to stir the contents of the tank.
  • a plurality of mixers disposed throughout the tank are used to stir the contents of the tank.
  • the mixer substantially mixes the contents of the equalization tank such that conditions (e.g., wastewater concentration and temperature) throughout the tank are uniform.
  • a first pump moves water from the equalization tank through a liquid-to-liquid heat exchanger.
  • the heat exchanger is controlled (e.g., by controlling the flow rate of fluid through the heat exchanger) such that wastewater exiting the heat exchanger is at a desired temperature for anaerobic treatment.
  • the desired temperature for anaerobic treatment can be between 40 °C to 60 °C.
  • the wastewater After exiting the heat exchanger, the wastewater enters one or more anaerobic reactors.
  • the concentration of sludge in each anaerobic reactor is the same as the overall concentration of sludge in the wastewater.
  • the anaerobic reactor has a higher concentration of sludge than the overall concentration of sludge in the wastewater.
  • a nutrient solution containing nitrogen and phosphorus is metered into each anaerobic reactor containing wastewater.
  • the nutrient solution reacts with the sludge in the anaerobic reactor to produce biogas which can contain 50% methane and have a heating value of approximately 12,000 British thermal units, or Btu, per pound).
  • the biogas exits each anaerobic reactor through a vent and flows into a manifold, where a plurality of biogas streams are combined into a single stream.
  • a compressor moves the stream of biogas to a boiler or a combustion engine as described in further detail below.
  • the compressor also moves the single stream of biogas through a desulphurization catalyst. Additionally or alternatively, the compressor can move the single stream of biogas through a sediment trap.
  • a second pump moves anaerobic effluent from the anaerobic reactors to one or more aerobic reactors (e.g., activated sludge reactors).
  • An aerator is disposed within each aerobic reactor to mix the anaerobic effluent, sludge, oxygen (e.g., oxygen contained in air).
  • oxygen e.g., oxygen contained in air.
  • oxidation of cellular material in the anaerobic effluent produces carbon dioxide, water, and ammonia.
  • Aerobic effluent moves (e.g., via gravity) to a separator, where sludge is separated from treated water. Some of the sludge is returned to the one or more aerobic reactors to create an elevated sludge concentration in the aerobic reactors, thereby facilitating the aerobic breakdown of cellular material in the wastewater.
  • a conveyor removes excess sludge from the separator. As described in further detail below, the excess sludge is used as fuel to create steam and/or electricity.
  • treated water is pumped from the separator to a settling tank. Solids dispersed throughout the treated water settle to the bottom of the settling tank and are subsequently removed. After a settling period, treated water is pumped from the settling tank through a fine filter to remove any additional solids remaining in the water. In some embodiments, chlorine is added to the treated water to kill pathogenic bacteria. In some embodiments, one or more physical-chemical separation techniques are used to further purify the treated water. For example, treated water can be pumped through a carbon adsorption reactor. As another example, treated water can pumped through a reverse osmosis reactor.
  • the production of alcohol from biomass can result in the production of various by-product streams useful for generating steam and electricity to be used in other parts of the plant.
  • steam generated from burning by-product streams can be used in the distillation process.
  • electricity generated from burning by-product streams can be used to power electron beam generators and ultrasonic transducers used in pretreatment.
  • the by-products used to generate steam and electricity are derived from a number of sources throughout the process.
  • anaerobic digestion of wastewater produces a biogas high in methane and a small amount of waste biomass (sludge).
  • post-distillate solids e.g., unconverted lignin, cellulose, and hemicellulose remaining from the pretreatment and primary processes
  • the biogas is diverted to a combustion engine connected to an electric generator to produce electricity.
  • the biogas can be used as a fuel source for a spark-ignited natural gas engine.
  • the biogas can be used as a fuel source for a direct-injection natural gas engine.
  • the biogas can be used as a fuel source for a combustion turbine.
  • the combustion engine can be configured in a cogeneration configuration. For example, waste heat from the combustion engines can be used to provide hot water or steam throughout the plant.
  • the sludge, and post-distillate solids are burned to heat water flowing through a heat exchanger.
  • the water flowing through the heat exchanger is evaporated and superheated to steam.
  • the steam is used in the pretreatment rector and in heat exchange in the distillation and evaporation processes. Additionally or alternatively, the steam expands to power a multi-stage steam turbine connected to an electric generator. Steam exiting the steam turbine is condensed with cooling water and returned to the heat exchanger for reheating to steam.
  • the flow rate of water through the heat exchanger is controlled to obtain a target electricity output from the steam turbine connected to an electric generator. For example, water can be added to the heat exchanger to ensure that the steam turbine is operating above a threshold condition (e.g., the turbine is spinning fast enough to turn the electric generator).
  • the biogas can be passed through a fuel reformer to produce hydrogen.
  • the hydrogen is then converted to electricity through a fuel cell.
  • biogas is described as being burned apart from the sludge and post-distillate solids, in certain embodiments, all of the waste by-products can be burned together to produce steam.
  • the alcohol produced can be a monohydroxy alcohol, e.g., ethanol, or a polyhydroxy alcohol, e.g., ethylene glycol or glycerin.
  • examples of alcohols that can be produced include methanol, ethanol, propanol, isopropanol, butanol, e.g., n-, sec- or t-butanol, ethylene glycol, propylene glycol, 1, 4-butane diol, glycerin or mixtures of these alcohols.
  • Each of the alcohols produced by the plant have commercial value as industrial feedstock.
  • ethanol can be used in the manufacture of varnishes and perfume.
  • methanol can be used as a solvent used as a component in windshield wiper fluid.
  • butanol can be used in plasficizers, resins, lacquers, and brake fluids.
  • Bioethanol produced by the plant is valuable as an ingredient used in the food and beverage industry.
  • the ethanol produced by the plant can be purified to food grade alcohol and used as a primary ingredient in the alcoholic beverages.
  • Bioethanol produced by the plant also has commercial value as a transportation fuel.
  • the use of ethanol as a transportation fuel can be implemented with relatively little capital investment from spark ignition engine manufacturers and owners (e.g., changes to injection timing, fuel-to-air ratio, and components of the fuel injection system).
  • Many automotive manufacturers currently offer flex-fuel vehicles capable of operation on ethanol/gasoline blends up to 85% ethanol by volume (e.g., standard equipment on a Chevy Tahoe 4 x 4).
  • Bioethanol produced by this plant can be used as an engine fuel to improve environmental and economic conditions beyond the location of the plant.
  • ethanol produced by this plant and used as a fuel can reduce greenhouse gas emissions from manmade sources (e.g., transportation sources).
  • ethanol produced by this plant and used as an engine fuel can also displace consumption of gasoline refined from oil.
  • Bioethanol strategies are discussed, e.g., by DiPardo in Journal of Outlook for Biomass Ethanol Production and Demand (EIA Forecasts), 2002 ; Sheehan in Biotechnology Progress, 15:8179,1999 ; Martin in Enzyme Microbes Technology, 31:274, 2002 ; Greer in BioCycle, 61-65, April 2005 ; Lynd in Microbiology and Molecular Biology Reviews, 66:3, 506-577, 2002 ; Ljungdahl et al. in U.S. Patent No. 4,292,406 ; and Bellamy in U.S. Patent No. 4,094,742 .
  • the organic acids produced can include monocarboxylic acids or a polycarboxylic acids.
  • organic acids include formic acid, acetic acid, propionic acid, butyric acid, valeric acid, caproic, palmitic acid, stearic acid, oxalic acid, malonic acid, succinic acid, glutaric acid, oleic acid, linoleic acid, glycolic acid, lactic acid, ⁇ -hydroxybutyric acid or mixtures of these acids.
  • all or a portion of the fermentation process can be interrupted before the cellulosic material is completely converted to ethanol.
  • the intermediate fermentation products include high concentrations of sugar and carbohydrates. These intermediate fermentation products can be used in preparation of food for human or animal consumption. In some embodiments, irradiation pretreatment of the cellulosic material will render the intermediate fermentation products sterile (e.g., fit for human consumption). In some embodiments, the intermediate fermentation products will require post-processing prior to use as food. For example, a dryer can be used to remove moisture from the intermediate fermentation products to facilitate storage, handling, and shelf-life. Additionally or alternatively, the intermediate fermentation products can be ground to a fine particle size in a stainless-steel laboratory mill to produce a flour-like substance.
  • Distillers grains and solubles can be converted into a valuable byproduct of the distillation-dehydration process. After the distillation-dehydration process, distillers grains and solubles can be dried to improve the ability to store and handle the material.
  • the resulting dried distillers grains and solubles is low in starch, high in fat, high in protein, high in fiber, and high in phosphorous.
  • DDGS can be valuable as a source of animal feed (e.g., as a feed source for dairy cattle).
  • DDGS can be subsequently combined with nutritional additives to meet specific dietary requirements of specific categories of animals (e.g., balancing digestible lysine and phosphorus for swine diets).
  • sonication can stimulate bioactivity and/or bioavailabilty of the medicinal components of plants with medicinal properties.
  • irradiation stimulates bioactivity and/or bioavailabilty of the medicinal components of plants with medicinal properties.
  • sonication and irradiation can be combined in the pretreatment of willow bark to stimulate the production of salicin.
  • intermediate fermentation products e.g., products that include high concentrations of sugar and carbohydrates
  • intermediate fermentation products can be supplemented with calcium create a nutriceutical that provides energy and helps improve or maintain bone strength.
  • lignin containing residues from primary and pretreatment processes has value as a high/medium energy fuel and can be used to generate power and steam for use in plant processes.
  • lignin residues are a new type of solids fuel and there is little demand for it outside of the plant boundaries, and the costs of drying it for transportation only subtract from its potential value.
  • gasification of the lignin residues can converting it to a higher-value product with lower cost.
  • a 1500 pound skid of virgin, half-gallon juice cartons made of un-printed polycoated white Kraft board having a bulk density of 20 lb/ft 3 was obtained from International Paper. Each carton was folded flat, and then fed into a 3 hp Flinch Baugh shredder at a rate of approximately 15 to 20 pounds per hour.
  • the shredder was equipped with two 12 inch rotary blades, two fixed blades and a 0.30 inch discharge screen. The gap between the rotary and fixed blades was adjusted to 0.10 inch.
  • the output from the shredder resembled confetti having a width of between 0.1 inch and 0.5 inch, a length of between 0.25 inch and 1 inch and a thickness equivalent to that of the starting material (about 0.075 inch).
  • the confetti-like material was fed to a Munson rotary knife cutter, Model SC30.
  • Model SC30 is equipped with four rotary blades, four fixed blades, and a discharge screen having 1/8 inch openings.
  • the gap between the rotary and fixed blades was set to approximately 0.020 inch.
  • the rotary knife cutter sheared the confetti-like pieces across the knife-edges, tearing the pieces apart and releasing a fibrous material at a rate of about one pound per hour.
  • the fibrous material had a BET surface area of 0.9748 m 2 /g +/- 0.0167 m 2 /g, a porosity of 89.0437 percent and a bulk density (@0.53 psia) of 0.1260 g/mL.
  • An average length of the fibers was 1.141 mm and an average width of the fibers was 0.027 mm, giving an average L/D of 42:1.
  • a scanning electron micrograph of the fibrous material is shown in FIG. 26
  • a 1500 pound skid of virgin bleached white Kraft board having a bulk density of 30 lb/ft 3 was obtained from International Paper.
  • the material was folded flat, and then fed into a 3 hp Flinch Baugh shredder at a rate of approximately 15 to 20 pounds per hour.
  • the shredder was equipped with two 12 inch rotary blades, two fixed blades and a 0.30 inch discharge screen. The gap between the rotary and fixed blades was adjusted to 0.10 inch.
  • the output from the shredder resembled confetti having a width of between 0.1 inch and 0.5 inch, a length of between 0.25 inch and 1 inch and a thickness equivalent to that of the starting material (about 0.075 inch).
  • a 1500 pound skid of virgin bleached white Kraft board having a bulk density of 30 lb/ft 3 was obtained from International Paper.
  • the material was folded flat, and then fed into a 3 hp Flinch Baugh shredder at a rate of approximately 15 to 20 pounds per hour.
  • the shredder was equipped with two 12 inch rotary blades, two fixed blades and a 0.30 inch discharge screen. The gap between the rotary and fixed blades was adjusted to 0.10 inch.
  • the output from the shredder resembled confetti (as above).
  • the confetti-like material was fed to a Munson rotary knife cutter, Model SC30.
  • the discharge screen had 1/16 inch openings.
  • the gap between the rotary and fixed blades was set to approximately 0.020 inch.
  • the rotary knife cutter the confetti-like pieces, releasing a fibrous material at a rate of about one pound per hour.
  • the material resulting from the first shearing was fed back into the same setup described above and sheared again.
  • the resulting fibrous material had a BET surface area of 1.4408 m 2 /g +/-0.0156 m 2 /g, a porosity of 90.8998 percent and a bulk density (@0.53 psia) of 0.1298 g/mL.
  • An average length of the fibers was 0.891 mm and an average width of the fibers was 0.026 mm, giving an average L/D of 34:1.
  • a scanning electron micrograph of the fibrous material is shown in FIG 28 at 25 X magnification.
  • a 1500 pound skid of virgin bleached white Kraft board having a bulk density of 30 lb/ft 3 was obtained from International Paper.
  • the material was folded flat, and then fed into a 3 hp Flinch Baugh shredder at a rate of approximately 15 to 20 pounds per hour.
  • the shredder was equipped with two 12 inch rotary blades, two fixed blades and a 0.30 inch discharge screen. The gap between the rotary and fixed blades was adjusted to 0.10 inch.
  • the output from the shredder resembled confetti (as above).
  • the confetti-like material was fed to a Munson rotary knife cutter, Model SC30.
  • the discharge screen had 1/8 inch openings.
  • the gap between the rotary and fixed blades was set to approximately 0.020 inch.
  • Fibrous material was prepared according to Example 2. Approximately 1 lb of water was sprayed onto each 10 lb of fibrous material. The fibrous material was densified using a California Pellet Mill 1100 operating at 75 °C. Pellets were obtained having a bulk density ranging from about 7 lb/ft 3 to about 15 lb/ft 3 .
  • Fibrous material was prepared according to Example 2.
  • a 2 weight percent stock solution of POLYOX TM WSR N10 (polyethylene oxide) was prepared in water.
  • Fibrous material is prepared according to Example 4 .
  • the fibrous Kraft paper is densified according to Example 5.
  • the densified pellets are placed in a glass ampoule having a maximum capacity of 250 mL.
  • the glass ampoule is evacuated under high vacuum (10 -5 torr) for 30 minutes, and then back-filled with argon gas.
  • the ampoule is sealed under argon.
  • the pellets in the ampoule are irradiated with gamma radiation for about 3 hours at a dose rate of about 1 Mrad per hour to provide an irradiated material in which the cellulose has a lower molecular weight than the fibrous Kraft starting material.
  • Fibrous material is prepared according to Example 4.
  • the fibrous Kraft paper is densified according to Example 5.
  • the densified pellets are placed in a glass ampoule having a maximum capacity of 250 mL.
  • the glass ampoule is sealed under an atmosphere of air.
  • the pellets in the ampoule are irradiated with gamma radiation for about 3 hours at a dose rate of about 1 Mrad per hour to provide an irradiated material in which the cellulose has a lower molecular weight than the fibrous Kraft starting material.
  • Sample materials presented in the following tables include Kraft paper (P), wheat straw (WS), alfalfa (A), and switchgrass (SG).
  • the number “132” of the Sample ID refers to the particle size of the material after shearing through a 1/32 inch screen.
  • the number after the dash refers to the dosage of radiation (MRad) and "US” refers to ultrasonic treatment.
  • a sample ID "P132-10” refers to Kraft paper that has been sheared to a particle size of 132 mesh and has been irradiated with 10 MRad. Table 1.
  • GPC Gel Permeation Chromatography
  • a distribution of molecular weights rather than a unique molecular weight is used to characterize synthetic polymers. To characterize this distribution, statistical averages are utilized. The most common of these averages are the “number average molecular weight” (M n ) and the “weight average molecular weight” (M w ).
  • the polydispersity index or PI is defined as the ratio of M w /M n .
  • the lowest value that a PI can be is 1. This represents a monodisperse sample; that is, a polymer with all of the molecules in the distribution being the same molecular weight.
  • the peak molecular weight value (M p ) is another descriptor defined as the mode of the molecular weight distribution. It signifies the molecular weight that is most abundant in the distribution. This value also gives insight to the molecular weight distribution.
  • the lignocellulosic samples required sample preparation prior to GPC analysis.
  • a saturated solution (8.4% by weight) of lithium chloride (LiCl) was prepared in dimethyl acetamide (DMAc).
  • DIc dimethyl acetamide
  • Approximately 100 mg of the sample was added to approximately 10 g of a freshly prepared saturated LiCl/DMAc solution, and the mixture was heated to approximately 150°C-170°C with stirring for 1 hour.
  • the resulting solutions were generally light- to dark-yellow in color.
  • the temperature of the solutions were decreased to approximately 100°C and heated for an additional 2 hours.
  • the temperature of the solutions were then decreased to approximately 50°C and the sample solution was heated for approximately 48 to 60 hours.
  • samples irradiated at 100 MRad were more easily solubilized as compared to their untreated counterpart. Additionally, the sheared samples (denoted by the number 132) had slightly lower average molecular weights as compared with uncut samples.
  • the resulting sample solutions were diluted 1:1 using DMAc as solvent and were filtered through a 0.45 ⁇ m PTFE filter.
  • the filtered sample solutions were then analyzed by GPC.
  • the peak average molecular weight (Mp) of the samples, as determined by Gel Permeation Chromatography (GPC), are summarized in Tables 1 and 2.Each sample was prepared in duplicate and each preparation of the sample was analyzed in duplicate (two injections) for a total of four injections per sample.
  • the EasiCal polystyrene standards PS1A and PS1B were used to generate a calibration curve for the molecular weight scale from about 580 to 7,500,00 Daltons. Table 3.
  • Example 10- Determing Cyrstallinity of Irradiated Material by X-Ray Diffraction
  • X-ray diffraction is a method by which a crystalline sample is irradiated with monoenergetic x-rays. The interaction of the lattice structure of the sample with these x-rays is recorded and provides information about the crystalline structure being irradiated. The resulting characteristic "fingerprint" allows for the identification of the crystalline compounds present in the sample. Using a whole-pattern fitting analysis (the Rietvelt Refinement), it is possible to perform quantitative analyses on samples containing more than one crystalline compound. Table 4.
  • XRD Data including Domain Size and % Crystallinity Sample ID Domain Size ( ⁇ ) % Crystallinity P132 55 55 P132-10 46 58 P132-100 50 55 P132-181 48 52 P132-US 26 40 A132 28 42 A132-10 26 40 A132-100 28 35 WS132 30 36 WS132-10 27 37 WS132-100 30 41 SG132 29 40 SG132-10 28 38 SG132-100 28 37 SG132-10-US 25 42 SG132-100-US 21 34
  • the distinguishing feature among the 20 samples is the peak breadth, which is related to the crystallite domain size.
  • the experimental peak breadth was used to compute the domain size and percent crystallinity and are reported in Table 4.
  • Mercury pore size and pore volume analysis (Table 5) is based on forcing mercury (a non-wetting liquid) into a porous structure under tightly controlled pressures. Since mercury does not wet most substances and will not spontaneously penetrate pores by capillary action, it must be forced into the voids of the sample by applying external pressure. The pressure required to fill the voids is inversely proportional to the size of the pores. Only a small amount of force or pressure is required to fill large voids, whereas much greater pressure is required to fill voids of very small pores. Table 5.
  • the AutoPore 9520 can attain a maximum pressure of 414 MPa or 60,000 psia.
  • the sample is placed in a bowl-like apparatus called a penetrometer, which is bonded to a glass capillary stem with a metal coating. As mercury invades the voids in and around the sample, it moves down the capillary stem. The loss of mercury from the capillary stem results in a change in the electrical capacitance.
  • the change in capacitance during the experiment is converted to volume of mercury by knowing the stem volume of the penetrometer in use.
  • a variety of penetrometers with different bowl (sample) sizes and capillaries are available to accommodate most sample sizes and configurations. Table 6 below defines some of the key parameters calculated for each sample. Table 6. Definition of Parameters Parameter Description
  • Total Intrusion Volume The total volume of mercury intruded during an experiment. This can include interstitial filling between small particles, porosity of sample, and compression volume of sample.
  • Total Pore Area The total intrusion volume converted to an area assuming cylindrical shaped pores.
  • Median Pore Diameter (volume) The size at the 50 th percentile on the cumulative volume graph.
  • Particle size was determined by Laser Light Scattering (Dry Sample Dispersion) using a Malvern Mastersizer 2000 using the following conditions: Feed Rate: 35% Disperser Pressure: 4 Bar Optical Model: (2.610, 1.000i) 1.000
  • sample was introduced onto a vibratory tray.
  • the feed rate and air pressure were adjusted to ensure that the particles were properly dispersed.
  • the key component is selecting an air pressure that will break up agglomerations, but does not compromise the sample integrity.
  • the amount of sample needed varies depending on the size of the particles. In general, samples with fine particles require less material than samples with coarse particles.
  • the pressure and quantity define a gas adsorption isotherm and are used to calculate a number of parameters, including BET surface area (Table 8).
  • Fiber length distribution testing was performed in triplicate on the samples submitted using the Techpap MorFi LB01 system. The average length and width are reported in Table 9. Table 9. Summary of Lignocellulosic Fiber Length and Width Data Sample ID Arithmetic Average (mm) Average Length weighted in Length (mm) Statistical Corrected Average Length Weighted in Length (mm) Width (micrometers) P132-10 0.484 0.615 0.773 24.7 P132-100 0.369 0.423 0.496 23.8 P132-181 0.312 0.342 0.392 24.4 A132-10 0.382 0.423 0.650 43.2 A132-100 0.362 0.435 0.592 29.9 SG132-10 0.328 0.363 0.521 44.0 SG132-100 0.325 0.351 0.466 43.8 WS132-10 0.353 0.381 0.565 44.7 WS132-100 0.354 0.371 0.536 45.4
  • Switchgrass was sheared according to Example 4.
  • the switchgrass was treated by ultrasound alone or irradiation with 10 Mrad or 100 Mrad of gamma rays, and then sonicated.
  • the resulting materials correspond to G132-BR (un-irradiated), G132-10-BR (10 Mrad and sonication) and G132-100-BR (100 Mrad and sonication), as presented in Table 1.
  • Sonication was performed on each sample for 30 minutes using 20kHz ultrasound from a 1000W horn under re-circulating conditions. Each sample was dispersed in water at a concentration of about 0.10 g/mL.
  • FIGS. 30 and 31 show the apparatus used for sonication.
  • Apparatus 500 includes a converter 502 connected to booster 504 communicating with a horn 506 fabricated from titanium or an alloy of titanium.
  • the horn which has a seal 510 made from VITON ® about its perimeter on its processing side, forms a liquid tight seal with a processing cell 508.
  • the processing side of the horn is immersed in a liquid, such as water, that has dispersed therein the sample to be sonicated. Pressure in the cell is monitored with a pressure gauge 512.
  • each sample is moved by pump 517 from tank 516 through the processing cell and is sonicated. After, sonication, the sample is captured in tank 520.
  • the process can be reversed in that the contents of tank 520 can be sent through the processing cell and captured in tank 516.
  • This process can be repeated a number of times until a desired level of processing is delivered to the sample.
  • Example 18 Scanning Electron Micrographs of Un-irradiated Switchgrass in Comparison to irradiated and Irradiated and Sonicated Switchgrass
  • Switchgrass samples for the scanning electron micrographs were applied to carbon tape and gold sputter coated (70 seconds). Images were taken with a JEOL 6500 field emission scanning electron microscope.
  • FIG. 32 is a scanning electron micrograph at 1000 X magnification of a fibrous material produced from shearing switchgrass on a rotary knife cutter, and then passing the sheared material through a 1/32 inch screen.
  • FIGS. 33 and 34 are scanning electron micrographs of the fibrous material of FIG. 32 after irradiation with 10 Mrad and 100 Mrad gamma rays, respectively, at 1000 X magnification.
  • FIG. 35 is a scanning electron micrographs of the fibrous material of FIG. 32 after irradiation with 10 Mrad and sonicaiton at 1000 X magnification.
  • FIG. 36 is a scanning electron micrographs of the fibrous material of FIG. 32 after irradiation with 100 Mrad and sonicaiton at 1000 X magnification.
  • Example 17 Infrared Spectrum of Irradiated Kraft Paper In Comparison to Un-irradiated Kraft Paper
  • FIG 37 is an infrared spectrum of Kraft board paper sheared according to Example 4, while FIG. 38 is an infrared spectrum of the Kraft paper of FIG 38 after irradiation with 100 Mrad of gamma radiation.
  • the irradiated sample shows an additional peak in region A (centered about 1730 cm -1 ) that is not found in the un-irradiated material.
  • Switchgrass is used as the feedstock and is sheared with a Munson rotary knife cutter into a fibrous material.
  • the fibrous material is then evenly distributed onto an open tray composed of tin with an area of greater than about 500 in2.
  • the fibrous material is distributed so that it has a depth of about 1- 2 inches in the open tray.
  • the fibrous material may be distributed in plastic bags at lower doses of irradiation (under 10 MRad), and left uncovered on the metal tray at higher doses of radiation.
  • the sonication device includes a converter connected to booster communicating with a horn fabricated from titanium or an alloy of titanium.
  • the horn which has a seal made from VITON® about its perimeter on its processing side, forms a liquid tight seal with a processing cell.
  • the processing side of the horn is immersed in a liquid, such as water, into which the irradiated fibrous material to be sonicated is immersed.
  • Pressure in the cell is monitored with a pressure gauge. In operation, each sample is moved by pump through the processing cell and is sonicated.
  • the irradiated fibrous material is removed from any container (e.g., plastic bags) and is dispersed in water at a concentration of about 0.10 g/mL. Sonication is performed on each sample for 30 minutes using 20 kHz ultrasound from a 1000 W horn under re-circulating conditions. After sonication, the irradiated fibrous material is captured in a tank. This process can be repeated a number of times until a desired level of processing is achieved based on monitoring the structural changes in the switchgrass. Again, some irradiated samples are kept under the same conditions as the remaining samples, but are not sonicated, to serve as controls. In addition, some samples that were not irradiated are sonicated, again to serve as controls. Thus, some controls are not processed, some are only irradiated, and some are only sonicated.
  • Specific lignocellulosic materials pretreated as described herein are analyzed for toxicity to common strains of yeast and bacteria used in the biofuels industry for the fermentation step in ethanol production. Additionally, sugar content and compatibility with cellulase enzymes are examined to determine the viability of the treatment process. Testing of the pretreated materials is carried out in two phases as follows.
  • Toxicity of the pretreated grasses and paper feedstocks is measured in yeast Saccharomyces cerevisiae (wine yeast) and Pichia stipitis (ATCC 66278) as well as the bacteria Zymomonas mobilis (ATCC 31821) and Clostridium thermocellum (ATCC 31924).
  • a growth study is performed with each of the organisms to determine the optimal time of incubation and sampling.
  • Each of the feedstocks is then incubated, in duplicate, with S. cerevisiae, P. stipitis, Z . mobilis, and C . thermocellum in a standard microbiological medium for each organism.
  • YM broth is used for the two yeast strains, S. cerevisiae and P. stipitis.
  • RM medium is used for Z . mobilis and CM4 medium for C . thermocellum.
  • a positive control, with pure sugar added, but no feedstock, is used for comparison.
  • a total of five samples is taken over a 12 hour period at time 0, 3, 6, 9, and 12 hours and analyzed for viability (plate counts for Z. mobilis and direct counts for S. cerevisiae ) and ethanol concentration.
  • Feedstocks are tested, in duplicate, with commercially available AccelleraseTM 1000, which contains a complex of enzymes that reduces lignocellulosic biomass into fermentable sugars.”
  • AccelleraseTM 1000 contains a complex of enzymes that reduces lignocellulosic biomass into fermentable sugars.
  • Trichoderma reesei and Aspergillus nidulans at the recommended temperature and concentration in an Erlenmeyer flask.
  • the flasks are incubated with moderate shaking at around 200 rpm for 12 hours. During that time, samples are taken every three hours at time 0, 3, 6, 9, and 12 hours to determine the concentration of reducing sugars ( Hope and Dean, Biotech J., 1974, 144:403 ) in the liquid portion of the flasks.
  • the optimum size for biomass conversion plants is affected by factors including economies of scale and the type and availability of biomass used as feedstock. Increasing plant size tends to increase economies of scale associated with plant processes. However, increasing plant size also tends to increase the costs (e.g., transportation costs) per unit of biomass feedstock. Studies analyzing these factors suggest that the appropriate size for biomass conversion plants can range from 2000 to 10,000 dried tons of biomass feedstock per day. The plant described below is sized to process 2000 tons of dry biomass feedstock per day.
  • FIG. 39 shows a process schematic of a biomass conversion system configured to process switchgrass.
  • the feed preparation subsystem processes raw biomass feedstock to remove foreign objects and provide consistently sized particles for further processing.
  • the pretreatment subsystem changes the molecular structure (e.g., reduces the average molecular weight and the crystallinity) of the biomass feedstock by irradiating the biomass feedstock, mixing the irradiated the biomass feedstock with water to form a slurry, and applying ultrasonic energy to the slurry.
  • the irradiation and sonication convert the cellulosic and lignocellulosic components of the biomass feedstock into fermentable materials.
  • the primary process subsystem ferments the glucose and other low weight sugars present after pretreatment to form alcohols.
  • the selected design feed rate for the plant is 2,000 dry tons per day of switchgrass biomass.
  • the design feed is chopped and/or sheared switchgrass.
  • Biomass feedstock in the form of bales of switchgrass are received by the plant on truck trailers. As the trucks are received, they are weighed and unloaded by forklifts. Some bales are sent to on-site storage while others are taken directly to the conveyors. From there, the bales are conveyed to an automatic unwrapping system that cuts away the plastic wrapping and/or net surrounding the bales. The biomass feedstock is then conveyed past a magnetic separator to remove tramp metal, after which it is introduced to shredder-shearer trains where the material is reduced in size. Finally, the biomass feedstock is conveyed to the pretreatment subsystem.
  • the switchgrass bales are wrapped with plastic net to ensure they don't break apart when handled, and may also be wrapped in plastic film to protect the bale from weather.
  • the bales are either square or round. The bales are received at the plant from off-site storage on large truck trailers.
  • switchgrass Since switchgrass is only seasonally available, long-term storage is required to provide feed to the plant year-round. Long-term storage will likely consist of 400-500 acres of uncovered piled rows of bales at a location (or multiple locations) reasonably close to the ethanol plant. On-site short-term storage is provided equivalent to 72 hours of production at an outside storage area. Bales and surrounding access ways as well as the transport conveyors will be on a concrete slab. A concrete slab is used because of the volume of traffic required to deliver the large amount of biomass feedstock required. A concrete slab will minimize the amount of standing water in the storage area, as well as reduce the biomass feedstock's exposure to dirt. The stored material provides a short-term supply for weekends, holidays, and when normal direct delivery of material into the process is interrupted.
  • bales are off-loaded by forklifts and are placed directly onto bale transport conveyors or in the short-term storage area. Bales are also reclaimed from short-term storage by forklifts and loaded onto the bale transport conveyors.
  • Unwrapped bales are broken up using a spreader bar and then discharged onto a conveyor which passes a magnetic separator to remove metal prior to shredding.
  • a tramp iron magnet is provided to catch stray magnetic metal and a scalping screen removes gross oversize and foreign material ahead of multiple shredder-shearer trains, which reduce the biomass feedstock to the proper size for pretreatment.
  • the shredder-shearer trains include shredders and rotary knife cutters. The shredders reduce the size of the raw biomass feedstock and feed the resulting material to the rotary knife cutters. The rotary knife cutters concurrently shear the biomass feedstock and screen the resulting material.
  • Each silo can hold approximately 55,000 cubic feet of biomass feedstock ( ⁇ 3 hours of plant operation).
  • a conveyor belt carries the biomass feedstock from the feed preparation subsystem 110 to the pretreatment subsystem 114.
  • the biomass feedstock is irradiated using electron beam emitters, mixed with water to form a slurry, and subjected to the application of ultrasonic energy.
  • irradiation of the biomass feedstock changes the molecular structure (e.g., reduces the average molecular weight and the crystallinity) of the biomass feedstock.
  • Mixing the irradiated biomass feedstock into a slurry and applying ultrasonic energy to the slurry further changes the molecular structure of the biomass feedstock.
  • the radiation and sonication in sequence may have synergistic effects in that the combination of techniques appears to achieve greater changes to the molecular structure (e.g., reduces the average molecular weight and the crystallinity) than either technique can efficiently achieve on its own.
  • the irradiation may make the overall physical structure of the biomass feedstock more brittle.
  • the application of ultrasonic energy further changes the molecular structure (e.g., reduces the average molecular weight and the crystallinity) and also can reduce the size of biomass feedstock particles.
  • the conveyor belt 491 carrying the biomass feedstock into the pretreatment subsystem distributes the biomass feedstock into multiple feed streams (e.g., 50 feed streams) each leading to separate electron beam emitters 492.
  • the biomass feedstock is irradiated while it is dry.
  • Each feed stream is carried on a separate conveyor belt to an associated electron beam emitter.
  • Each irradiation feed conveyor belt can be approximately one meter wide.
  • a localized vibration is induced in each conveyor belt to evenly distribute the dry biomass feedstock over the cross-sectional width of the conveyor belt.
  • Electron beam emitter 492 e.g., electron beam irradiation devices commercially available from Titan Corporation, San Diego, CA
  • the electron beam emitters are scanning beam devices with a sweep width of 1 meter to correspond to the width of the conveyor belt.
  • electron beam emitters with large, fixed beam widths are used. Factors including belt/beam width, desired dose, biomass feedstock density, and power applied govern the number of electron beam emitters required for the plant to process 2,000 tons per day of dry feed.
  • the irradiated biomass feedstock is mixed with water to form a slurry before ultrasonic energy is applied.
  • the irradiated biomass feedstock is fed into a reservoir 1214 through a first intake 1232 and water is fed into the reservoir 1214 through second intake 1234.
  • Appropriate valves (manual or automated) control the flow of biomass feedstock and the flow of water to produce a desired ratio of biomass feedstock to water (e.g., 10% cellulosic material, weight by volume).
  • Each reservoir 1214 includes a mixer 1240 to agitate the contents of volume 1236 and disperse biomass feedstock throughout the water.
  • the slurry is pumped (e.g., using a recessed impeller vortex pump 1218) from reservoir 1214 to and through a flow cell 1224 including an ultrasonic transducer 1226.
  • pump 1218 is configured to agitate the slurry 1216 such that the mixture of biomass feedstock and water is substantially uniform at inlet 1220 of the flow cell 1224.
  • the pump 1218 can agitate the slurry 1216 to create a turbulent flow that persists throughout the piping between the first pump and inlet 1220 of flow cell 1224.
  • ultrasonic transducer 1226 transmits ultrasonic energy into slurry 1216 as the slurry flows through flow cell 1224.
  • Ultrasonic transducer 1226 converts electrical energy into high frequency mechanical energy (e.g., ultrasonic energy) which is then delivered to the slurry through booster 48.
  • Ultrasonic transducers are commercially available (e.g., from Hielscher USA, Inc. of Ringwood, New Jersey) that are capable of delivering a continuous power of 16 kilowatts.
  • the ultrasonic energy traveling through booster 1248 in reactor volume 1244 creates a series of compressions and rarefactions in process stream 1216 with an intensity sufficient to create cavitation in process stream 1216.
  • Cavitation disaggregates components of the biomass feedstock including, for example, cellulosic and lignocellulosic material dispersed in process stream 1216 (e.g., slurry). Cavitation also produces free radicals in the water of process stream 1216 (e.g., slurry). These free radicals act to further break down the cellulosic material in process stream 1216. In general, about 250 MJ/m 3 of ultrasonic energy is applied to process stream 1216 containing fragments of poplar chips.
  • process stream 1216 exits flow cell 24 through outlet 1222.
  • Flow cell 1224 also includes a heat exchanger 1246 in thermal communication with at least a portion of reactor volume 1244.
  • Cooling fluid 1248 e.g., water
  • process stream 1216 e.g., slurry
  • the flow of cooling fluid 1248 into heat exchanger 1246 is controlled to maintain an approximately constant temperature in reactor volume 1244.
  • the temperature of cooling fluid 1248 flowing into heat exchanger 1246 is controlled to maintain an approximately constant temperature in reactor volume 1244.
  • the outlet 1242 of flow cell 1224 is arranged near the bottom of reservoir 1214 to induce a gravity feed of process stream 1216 (e.g., slurry) out of reservoir 1214 towards the inlet of a second pump 1230 which pumps process stream 1216 (e.g., slurry) towards the primary process subsystem.
  • process stream 1216 e.g., slurry
  • Sonication systems can include a single flow path (as described above) or multiple parallel flow paths each with an associated individual sonication units. Multiple sonication units can also be arranged to series to increase the amount of sonic energy applied to the slurry.
  • a vacuum rotary drum type filter removes solids from the slurry before fermentation. Liquid from the filter is pumped cooled prior to entering the fermentors. Filtered solids are passed to passed to the post-processing subsystem for further processing.
  • the fermentation tanks are large, low pressure, stainless steel vessels with conical bottoms and slow speed agitators.
  • Multiple first stage fermentation tanks can be arranged in series.
  • the temperature in the first stage fermentation tanks is controlled to 30 degrees centigrade using external heat exchangers.
  • Yeast is added to the first stage fermentation tank at the head of each series of tanks and carries through to the other tanks in the series.
  • Second stage fermentation consists of two continuous fermentors in series. Both fermentors are continuously agitated with slow speed mechanical mixers. Temperature is controlled with chilled water in external exchangers with continuous recirculation. Recirculation pumps are of the progressive cavity type because of the high solids concentration.
  • Off gas from the fermentation tanks and fermentors is combined and washed in a counter-current water column before being vented to the atmosphere.
  • the off gas is washed to recover ethanol rather than for air emissions control.
  • Distillation and molecular sieve adsorption are used to recover ethanol from the raw fermentation beer and produce 99.5% ethanol. Distillation is accomplished in two columns-the first, called the beer column, removes the dissolved CO2 and most of the water, and the second concentrates the ethanol to a near azeotropic composition.
  • Fermentation vents (containing mostly CO2, but also some ethanol) as well as the beer column vent are scrubbed in a water scrubber, recovering nearly all of the ethanol.
  • the scrubber effluent is fed to the first distillation column along with the fermentation beer.
  • the bottoms from the first distillation contain all the unconverted insoluble and dissolved solids.
  • the insoluble solids are dewatered by a pressure filter and sent to a combustor.
  • the liquid from the pressure filter that is not recycled is concentrated in a multiple effect evaporator using waste heat from the distillation.
  • the concentrated syrup from the evaporator is mixed with the solids being sent to the combustor, and the evaporated condensate is used as relatively clean recycle water to the process.
  • an evaporator is included in the process.
  • the total amount of the water from the pressure filter that is directly recycled is set at 25%.
  • Organic salts like ammonium acetate or lactate, steep liquor components not utilized by the organism, or inorganic compounds in the biomass end up in this stream. Recycling too much of this material can result in levels of ionic strength and osmotic pressures that can be detrimental to the fermenting organism's efficiency.
  • the evaporator concentrates the dissolved solids into a syrup that can be sent to the combustor, minimizing the load to wastewater treatment.
  • the wastewater treatment section treats process water for reuse to reduce plant makeup water requirements.
  • Wastewater is initially screened to remove large particles, which are collected in a hopper and sent to a landfill. Screening is followed by anaerobic digestion and aerobic digestion to digest organic matter in the stream.
  • Anaerobic digestion produces a biogas stream that is rich in methane that is fed to the combustor. Aerobic digestion produces a relatively clean water stream for reuse in the process as well as a sludge that is primarily composed of cell mass. The sludge is also burned in the combustor.
  • This screening / anaerobic digestion / aerobic digestion scheme is standard within the current ethanol industry and facilities in the 1-5 million gallons per day range can be obtained as "off-the-shelf" units from vendors.
  • the purpose of the combustor, boiler, and turbogenerator subsystem is to burn various by-product streams for steam and electricity generation.
  • some lignin, cellulose, and hemicellulose remains unconverted through the pretreatment and primary processes.
  • the majority of wastewater from the process is concentrated to a syrup high in soluble solids.
  • Anaerobic digestion of the remaining wastewater produces a biogas high in methane. Aerobic digestion produces a small amount of waste biomass (sludge). Burning these by-product streams to generate steam and electricity allows the plant to be self sufficient in energy, reduces solid waste disposal costs, and generates additional revenue through sales of excess electricity.
  • Three primary fuel streams (post-distillate solids, biogas, and evaporator syrup) are fed to a circulating fluidized bed combustor.
  • the small amount of waste biomass (sludge) from wastewater treatment is also sent to the combustor.
  • a fan moves air into the combustion chamber.
  • Treated water enters the heat exchanger circuit in the combustor and is evaporated and superheated to 510°C (950°F) and 86 atm (1265 psia) steam.
  • Flue gas from the combustor preheats the entering combustion air then enters a baghouse to remove particulates, which are landfilled. The gas is exhausted through a stack.
  • a multistage turbine and generator are used to generate electricity. Steam is extracted from the turbine at three different conditions for injection into the pretreatment reactor and heat exchange in distillation and evaporation. The remaining steam is condensed with cooling water and returned to the boiler feedwater system along with condensate from the various heat exchangers in the process. Treated well water is used as makeup to replace steam used in direct injection.
  • relatively low doses of radiation optionally, combined with acoustic energy, e.g., ultrasound, are utilized to crosslink, graft, or otherwise increase the molecular weight of a natural or synthetic carbohydrate-containing material, such as any of those materials in any form (e.g., fibrous form) described herein, e.g., sheared or un-sheared cellulosic or lignocellulosic materials, such as cellulose.
  • a natural or synthetic carbohydrate-containing material such as any of those materials in any form (e.g., fibrous form) described herein, e.g., sheared or un-sheared cellulosic or lignocellulosic materials, such as cellulose.
  • the crosslinking, grafting, or otherwise increasing the molecular weight of the natural or synthetic carbohydrate-containing material can be performed in a controlled and predetermined manner by selecting the type or types of radiation employed (e.g., e-beam and ultraviolet or e-beam and gamma) and/or dose or number of doses of radiation applied.
  • a material having increased molecular weight can be useful in making a composite, such as a fiber-resin composite, having improved mechanical properties, such as abrasion resistance, compression strength, fracture resistance, impact strength, bending strength, tensile modulus, flexural modulus and elongation at break.
  • Crosslinking, grafting, or otherwise increasing the molecular weight of a selected material can improve the thermal stability of the material relative to an un-treated material. Increasing the thermal stability of the selected material can allow it to be processed at higher temperatures without degradation.
  • treating materials with radiation can sterilize the materials, which can reduce their tendency to rot, e.g., while in a composite.
  • the crosslinking, grafting, or otherwise increasing the molecular weight of a natural or synthetic carbohydrate-containing material can be performed in a controlled and predetermined manner for a particular application to provide optimal properties, such as strength, by selecting the type or types of radiation employed and/or dose or doses of radiation applied.
  • the combination of radiation e.g., low dose radiation
  • acoustic energy e.g., sonic or ultrasonic energy
  • the combination of radiation can improve material throughput and/or minimize energy usage.
  • the resin can be any thermoplastic, thermoset, elastomer, adhesive, or mixtures of these resins.
  • Suitable resins include any resin, or mixture of resins described herein.
  • the material having the increased molecular weight can be combined, blended, or added to other materials, such as metals, metal alloys, ceramics (e.g., cement), lignin, elastomers, asphalts, glass, or mixtures of any of these and/or resins.
  • fiber-reinforced cements can be produced having improved mechanical properties, such as the properties described herein, e.g., compression strength and/or fracture resistance.
  • Crosslinking, grafting, or otherwise increasing the molecular weight of a natural or synthetic carbohydrate-containing material utilizing radiation can provide useful materials in many forms and for many applications.
  • the carbohydrate-containing material can be in the form of a paper product, such as paper, paper pulp, or paper effluent, particle board, glued lumber laminates, e.g., veneer, or plywood, lumber, e.g., pine, poplar, oak, or even balsa wood lumber.
  • Treating paper, particle board, laminates or lumber can increase their mechanical properties, such as their strength. For example, treating pine lumber with radiation can make a high strength structural material.
  • radiation can be utilized at any point in its manufacture.
  • the pulp can be irradiated, a pressed fiber preform can be irradiated, or the finished paper itself can be irradiated.
  • radiation is applied at more than one point during the manufacturing process..
  • a fibrous material that includes a first cellulosic and/or lignocellulosic material having a first molecular weight can be irradiated in a manner to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight.
  • a dose of from about 0.2 Mrad to about 10 Mrad e.g., from about 0.5 Mrad to about 7.5 Mrad, or from about 2.0 Mrad to about 5.0 Mrad, can be applied.
  • a smaller dose can be utilized (relative to gamma radiation), such as a dose of from about 0.1 Mrad to about 5 Mrad, e.g., between about 0.2 Mrad to about 3 Mrad, or between about 0.25 Mrad and about 2.5 Mrad.
  • the second cellulosic and/or lignocellulosic material can be combined with a material, such as a resin, and formed into a composite, e.g., by compression molding, injection molding or extrusion. Forming resin-fiber composites is described in WO 2006/102543 . Once composites are formed, they can be irradiated to further increase the molecular weight of the carbohydrate-containing material while in the composite.
  • a fibrous material that includes a first cellulosic and/or lignocellulosic material having a first molecular weight can be combined with a material, such as a resin, to provide a composite, and then the composite can be irradiated with a relatively low dose of radiation so as to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight
  • a dose of from about 1 Mrad to about 10 Mrad can be applied.
  • a matrix such as a resin matrix.
  • the resin is a cross-linkable resin, and, as such, it crosslinks as the carbohydrate-containing material increases in molecular weight, which can provide a synergistic effect to provide maximum mechanical properties to a composite.
  • such composites can have excellent low temperature performance, e.g., having a reduced tendency to break and/or crack at low temperatures, e.g., temperatures below 0 °C, e.g., below -10 °C, -20 °C, -40 °C, -50 °C, -60 °C or even below -100 °C, and/or excellent performance at high temperatures, e.g., capable of maintaining their advantageous mechanical properties at relatively high temperature, e.g., at temperatures above 100 °C, e.g., above 125 °C, 150 °C, 200 °C, 250 °C, 300 °C, 400 °C, or even above 500 °C.
  • such composites can have excellent chemical resistance, e.g., resistance to swelling in a solvent, e.g., a hydrocarbon solvent, resistance to chemical attack, e.g., by strong acids, strong bases, strong oxidants (e.g., chlorine or bleach) or reducing agents (e.g., active metals such as sodium and potassium).
  • a solvent e.g., a hydrocarbon solvent
  • chemical attack e.g., by strong acids, strong bases, strong oxidants (e.g., chlorine or bleach) or reducing agents (e.g., active metals such as sodium and potassium).
  • the resin, or other matrix material does not crosslink during irradiation.
  • additional radiation is applied while the carbohydrate-containing material is within the matrix to further increase the molecular weight of the carbohydrate-containing material.
  • the radiation causes bonds to form between the matrix and the carbohydrate-containing material.
  • the carbohydrate-containing material is in the form of fibers.
  • the fibers when the fibers are utilized in a composite, the fibers can be randomly oriented within the matrix. In other embodiments, the fibers can be substantially oriented, such as in one, two, three or four directions. If desired, the fibers can be continuous or discrete.
  • Additives can be added, e.g., to the combination of a fibrous material and resin.
  • Additives include fillers such as calcium carbonate, graphite, wollastonite, mica, glass, fiber glass, silica, and talc; inorganic flame retardants such as alumina trihydrate or magnesium hydroxide; organic flame retardants such as chlorinated or brominated organic compounds; ground construction waste; ground tire rubber, carbon fibers; or metal fibers or powders (e.g., aluminum, stainless steel).
  • additives can reinforce, extend, or change electrical, mechanical or compatibility properties.
  • Other additives include lignin, fragrances, coupling agents, compatibilizers, e.g., maleated polypropylene, processing aids, lubricants, e.g., fluorinated polyethylene, plasticizers, antioxidants, opacifiers, heat stabilizers, colorants, foaming agents, impact modifiers, polymers, e.g., degradable polymers, photostabilizers, biocides, antistatic agents, e.g., stearates or ethoxylated fatty acid amines.
  • compatibilizers e.g., maleated polypropylene
  • processing aids e.g., lubricants, e.g., fluorinated polyethylene, plasticizers, antioxidants, opacifiers, heat stabilizers, colorants, foaming agents, impact modifiers, polymers, e.g., degradable polymers, photostabilizers, biocides
  • Suitable antistatic compounds include conductive carbon blacks, carbon fibers, metal fillers, cationic compounds, e.g., quaternary ammonium compounds, e.g., N-(3-chloro-2-hydroxypropyl)-trimethylammonium chloride, alkanolamides, and amines.
  • cationic compounds e.g., quaternary ammonium compounds, e.g., N-(3-chloro-2-hydroxypropyl)-trimethylammonium chloride, alkanolamides, and amines.
  • degradable polymers include polyhydroxy acids, e.g., polylactides, polyglycolides and copolymers of lactic acid and glycolic acid, poly(hydroxybutyric acid), poly(hydroxyvaleric acid), poly[lactide-co-(e-caprolactone)], poly[glycolide-co-(e-caprolactone)], polycarbonates, poly(amino acids), poly(hydroxyalkanoate)s, polyanhydrides, polyorthoesters and blends of these polymers.
  • polyhydroxy acids e.g., polylactides, polyglycolides and copolymers of lactic acid and glycolic acid, poly(hydroxybutyric acid), poly(hydroxyvaleric acid), poly[lactide-co-(e-caprolactone)], poly[glycolide-co-(e-caprolactone)], polycarbonates, poly(amino acids), poly(hydroxyalkanoate)s, polyanhydrides, polyorthoesters and blends of these
  • additives When described additives are included, they can be present in amounts, calculated on a dry weight basis, of from below 1 percent to as high as 80 percent, based on total weight of the fibrous material. More typically, amounts range from between about 0.5 percent to about 50 percent by weight, e.g., 5 percent, 10 percent, 20 percent, 30, percent or more, e.g., 40 percent.
  • any additives described herein can be encapsulated, e.g., spray dried or microencapsulated, e.g., to protect the additives from heat or moisture during handling.
  • the fibrous materials, densified fibrous materials, resins or additives may be dyed.
  • the fibrous material can be dyed before combining with the resin and compounding to form composites.
  • this dyeing can be helpful in masking or hiding the fibrous material, especially large agglomerations of the fibrous material, in molded or extruded parts, when this is desired.
  • Such large agglomerations when present in relatively high concentrations, can show up as speckles in the surfaces of the molded or extruded parts.
  • the desired fibrous material can be dyed using an acid dye, direct dye or a reactive dye.
  • dyes are available from Spectra Dyes, Kearny, NJ or Keystone Aniline Corporation, Chicago, IL.
  • Specific examples of dyes include SPECTRATM LIGHT YELLOW 2G, SPECTRACIDTM YELLOW 4GL CONC 200, SPECTRANYLTM RHODAMINE 8, SPECTRANYLTM NEUTRAL RED B, SPECTRAMINETM BENZOPERPURINE, SPECTRADIAZOTM BLACK OB, SPECTRAMINETM TURQUOISE G, and SPECTRAMINETM GREY LVL 200%, each being available from Spectra Dyes.
  • resin color concentrates containing pigments are blended with dyes. When such blends are then compounded with the desired fibrous material, the fibrous material may be dyed in-situ during the compounding. Color concentrates are available from Clariant.
  • the fragrance e.g., natural wood fragrance
  • the fragrance can be compounded into the resin used to make the composite.
  • the fragrance is compounded directly into the resin as an oil.
  • the oil can be compounded into the resin using a roll mill, e.g., a Banbury ® mixer or an extruder, e.g., a twin-screw extruder with counter-rotating screws.
  • a Banbury ® mixer is the F-Series Banbury ® mixer, manufactured by Farrel.
  • An example of a twin-screw extruder is the WP ZSK 50 MEGAcompunder TM , manufactured by Krupp Wemer & Pfleiderer.
  • the scented resin can be added to the fibrous material and extruded or molded.
  • master batches of fragrance-filled resins are available commercially from International Flavors and Fragrances, under the tradename PolyIff TM or from the RTP Company.
  • the amount of fragrance in the composite is between about 0.005 % by weight and about 10 % by weight, e.g., between about 0.1 % and about 5 % or 0.25 % and about 2.5 %.
  • fragrances include evergreen or redwood.
  • Other fragrances include peppermint, cherry, strawberry, peach, lime, spearmint, cinnamon, anise, basil, bergamot, black pepper, camphor, chamomile, citronella, eucalyptus, pine, fir, geranium, ginger, grapefruit, jasmine, juniperberry, lavender, lemon, mandarin, marjoram, musk, myrhh, orange, patchouli, rose, rosemary, sage, sandalwood, tea tree, thyme, wintergreen, ylang ylang, vanilla, new car or mixtures of these fragrances.
  • the amount of fragrance in the fibrous material-fragrance combination is between about 0.005 % by weight and about 20 % by weight, e.g., between about 0.1 % and about 5 % or 0.25 % and about 2.5 %.
  • inorganic fillers such as calcium carbonate (e.g., precipitated calcium carbonate or natural calcium carbonate), aragonite clay, orthorhombic clays, calcite clay, rhombohedral clays, kaolin, clay, bentonite clay, dicalcium phosphate, tricalcium phosphate, calcium pyrophosphate, insoluble sodium metaphosphate, precipitated calcium carbonate, magnesium orthophosphate, trimagnesium phosphate, hydroxyapatites, synthetic apatites, alumina, silica xerogel, metal aluminosilicate complexes, sodium aluminum silicates, zirconium silicate, silicon dioxide or combinations of the inorganic additives may be used.
  • the fillers can have, e.g., a particle size of greater than 1 micron, e.g., greater than 2
  • Nanometer scale fillers can also be used alone, or in combination with fibrous materials of any size and/or shape.
  • the fillers can be in the form of, e.g., a particle, a plate or a fiber.
  • nanometer sized clays, silicon and carbon nanotubes, and silicon and carbon nanowires can be used.
  • the filler can have a transverse dimension less than 1000 nm, e.g., less than 900 nm, 800 nm, 750 nm, 600 nm, 500 nm, 350 nm, 300 nm, 250 nm, 200 nm, less than 100 nm, or even less than 50 nm.
  • the nano-clay is a montmorillonite.
  • montmorillonite Such clays are available from Nanocor, Inc. and Southern Clay products, and have been described in U.S. Patent Nos. 6,849,680 and 6,737,464 .
  • the clays can be surface treated before mixing into, e.g., a resin or a fibrous material.
  • the clay can be surface is treated so that its surface is ionic in nature, e.g., cationic or anionic.
  • Aggregated or agglomerated nanometer scale fillers, or nanometer scale fillers that are assembled into supramolecular structures, e.g., self-assembled supramolecular structures can also be used.
  • the aggregated or supramolecular fillers can be open or closed in structure, and can have a variety of shapes, e.g., cage, tube or spherical.

Abstract

The invention relates to a method of making sugars comprising irradiating a layer of lignocellulosic material with a series of doses of radiation, using more than one electron beam device to deliver a total dose of radiation of at least 20 Mrad; and converting the irradiated material with an enzyme or micro-organism.

Description

    CROSS REFERENCE TO RELATED APPLICATIONS
  • This application claims priority from U.S. Provisional Application Serial No. 60/854,519, filed on October 26, 2006 , U.S. Provisional Application Serial No. 60/863,290, filed on October 27, 2006 , U.S. Provisional Application Serial No. 60/859,911, filed on November 17, 2006 , U.S. Provisional Application Serial No. 60/875,144, filed on December 15, 2006 , and U.S. Provisional Application Serial No. 60/881,891, filed on January 23, 2007 , the contents of each of which are incorporated herein by reference in their entireties.
  • TECHNICAL FIELD
  • This invention relates to processing biomass, and products made therefrom.
  • BACKGROUND
  • Cellulosic and lignocellulosic materials, e.g., in fibrous form, are produced, processed, and used in large quantities in a number of applications. Often such materials are used once, and then discarded as waste, or are simply considered to be waste materials, e.g., sewage, bagasse, sawdust, and stover.
  • Various cellulosic and lignocellulosic materials, their uses, and applications have been described in U.S. Patent Nos. 7,074,918 , 6,448,307 , 6,258,876 , 6,207,729 , 5,973,035 and 5,952,105 ; and in various patent applications, including "FIBROUS MATERIALS AND COMPOSITES," PCT/US2006/010648, filed on March 23, 2006 , AND "FIBROUS MATERIALS AND COMPOSITES," U.S. Patent Application Publication No. 2007/0045456 .
  • SUMMARY
  • Generally, this invention relates to carbohydrate-containing materials (e.g., biomass materials or biomass-derived materials), methods of making and processing such materials to change their structure, and products made from the structurally changed materials. For example, many of the methods described herein can provide cellulosic and/or lignocellulosic materials that have a lower molecular weight and/or crystallinity relative to a native material. Many of the methods provide materials that can be more readily utilized by a variety of microorganisms to produce useful products, such as hydrogen, alcohols (e.g., ethanol or butanol), organic acids (e.g., acetic acid), hydrocarbons, co-products (e.g., proteins) or mixtures of any of these.
  • In one aspect, the invention features methods of changing a molecular structure of a biomass feedstock that include preparing the biomass feedstock by reducing one or more dimensions of individual pieces of biomass; pretreating the biomass feedstock using two or more different pretreatment methods that each change the molecular structure, in which the different pretreatment methods are selected from radiation, sonication, pyrolysis, and oxidation; and processing the prepared and pretreated biomass feedstock to produce a product.
  • In some embodiments, the biomass feedstock is prepared and then pretreated. The biomass feedstock can also be pretreated and then prepared.
  • Reducing one or more dimensions of individual pieces of biomass can include, e.g., shearing, cutting, or grinding.
  • In some embodiments, the two or more pretreatment methods are applied to the biomass feedstock at or about the same time.
  • For example, the two or more pretreatment methods can include radiation and sonication. For example, the radiation can be in the form of an electron beam. In specific embodiments, the electron beam radiation is applied at a total dosage of about 10 MRad and the sonication is applied at a total energy of more than 5 MJ/m3. Radiation can precede sonication, or sonication can precede radiation, or radiation and sonication can performed at or about the same time.
  • For example, the change in molecular structure of the biomass feedstock can include a change in any one or more of an average molecular weight, average crystallinity, surface area, polymerization, porosity, branching, grafting, and domain size of the biomass. In some embodiments, the change in molecular structure of the biomass feedstock includes a decrease in either one or both of an average molecular weight and average crystallinity of the biomass or an increase in either one or both of surface area and porosity of the biomass.
  • In another aspect, the invention features methods of making products, such as combustible fuels, that include providing a material that includes a carbohydrate produced by a process that includes pretreating a biomass feedstock with any two or more of radiation, sonication, pyrolysis, and oxidation; and contacting the material with a microorganism having the ability to convert at least a portion, e.g., at least about 1 percent by weight, of the material to the product, such as a combustible fuel.
  • In some embodiments, the two or more different pretreatment methods include radiation and sonication, radiation and oxidation, radiation and pyrolization, sonication and oxidation, sonication and pyrolization, or oxidation and pyrolization.
  • For example, any method described herein can further include pretreating the biomass feedstock with steam explosion.
  • For example, in some embodiments, the process does not include hydrolyzing the biomass with an acid or a base.
  • In some embodiments, at least about seventy percent by weight of the biomass is unhydrolyzed, e.g., at least at 95 percent by weight of the biomass has not been hydrolyzed. In specific embodiments, substantially none of the biomass has been hydrolyzed.
  • For example, in some embodiments, at least one pretreatment method is performed on biomass in which less than about 25 percent by weight of the biomass is wetted with a liquid, such as water. Specifically, in some embodiments, at least one pretreatment method is performed on biomass in which substantially none of the biomass is wetted with a liquid, such as water.
  • The biomass can have, e.g., less than about five percent by weight retained water, measured at 25°C and at fifty percent relative humidity.
  • In some embodiments, at least one pretreatment method can be performed on biomass in which less than about 25 percent by weight of the biomass is in a swollen state, the swollen state being characterized as having a volume of more than about 2.5 percent higher than an unswollen state. In other embodiments, the biomass is mixed with or includes a swelling agent.
  • For example, in any method described herein, the biomass can be mixed with or and include a swelling agent, and the biomass can receives a dose of less than about 10 Mrad of radiation.
  • In some embodiments, one of the pretreatment methods is or includes radiation.
  • In some embodiments, at least one of the pretreatment methods, e.g., radiation, is performed on the biomass feedstock while the biomass feedstock is exposed to air.
  • Pressure can be utilized. For example, at least one of the pretreatment methods, e.g., radiation, can be performed on the biomass under a pressure of greater than about 2.5 atmospheres, such as greater than 5 or 10 atmospheres.
  • The process can further include oxidizing, pyrolizing, or steam exploding the biomass.
  • Examples of biomass feedstock include paper, paper products, paper waste, wood, particle board, sawdust, agricultural waste, sewage, silage, grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, corn stover, switchgrass, alfalfa, hay, rice hulls, coconut hair, cotton, synthetic celluloses, seaweed, algae, or mixtures of these.
  • The biomass can be or can include a natural or a synthetic material.
  • Examples of fuels include one or more of hydrogen, alcohols, and hydrocarbons: For example, the alcohols can be ethanol, n-propanol, isoproanol, n-butanol, or mixtures of these.
  • The microorganism can be, e.g., a bacterium or a yeast.
  • Converting can include fermenting the material to the product, such as the combustible fuel.
  • Irradiation can be, e.g., performed utilizing an ionizing radiation, such as gamma rays, a beam of electrons, or ultraviolet C radiation having a wavelength of from about 100 nm to about 280 nm.
  • The ionizing radiation can include electron beam radiation.
  • For example, the radiation can be applied at a total dose of between about 10 Mrad and about 150 Mrad, such as at a dose rate of about 0.5 to about 10 Mrad/day, or 1 Mrad/s to about 10 Mrad/s.
  • In some embodiments, irradiating includes applying two or more radiation sources, such as gamma rays and a beam of electrons.
  • For example, sonication can be performed at a frequency of between about 15 kHz and about 25 kHz, such as between about 18 kHz and 22 kHz.
  • In some embodiments, the biomass includes a first cellulose having a first number average molecular weight and the carbohydrate material comprises a second cellulose having a second number average molecular weight lower than the first number average molecular weight. For example, the second number average molecular weight is lower than the first number average molecular weight by more than about one-fold. In some embodiments, the first cellulose has a first crystallinity, and the second cellulose has a second crystallinity lower than the first crystallinity. For example, the second crystallinity can be lower than the first crystallinity by more than about 10 percent.
  • In some embodiments, the first cellulose can have a first level of oxidation and the second cellulose has a second level of oxidation higher than the first level of oxidation.
  • For example, the biomass feedstock can be prepared by shearing a biomass fiber source to provide a fibrous material. For example, the shearing can be performed with a rotary knife cutter. The fibers of the fibrous material can have, e.g., an average length-to-diameter ratio of greater than 5/1. The fibrous material can have, e.g., a BET surface area of greater than 0.25 m2/g.
  • In some embodiments, the carbohydrate can include one or more β-1,4-linkages and having a number average molecular weight between about 3,000 and 50,000.
  • For example, the pretreated biomass material can further include a buffer, such as sodium bicarbonate or ammonium chloride, an electrolyte, such as potassium chloride or sodium chloride a growth factor, such as biotin and/or a base pair such as uracil, a surfactant, a mineral, or a chelating agent.
  • In some embodiments, the biomass feedstock is pretreated using any three or more of radiation, sonication, pyrolysis, and oxidation, in any order, or at about the same time.
  • In another aspect, the invention features methods of making a product, such as a combustible fuel that includes providing a material that includes a carbohydrate produced by pretreating a biomass feedstock with any one or more of radiation, sonication, oxidation, pyrolysis, and steam explosion, in which less than about 25 percent by weight of the biomass is in a swollen state, the swollen state being characterized as having a volume of more than about 2.5 percent higher than a nominal, unswollen state; and contacting the material with a microorganism having the ability to convert at least a portion, e.g., at least about 1 percent by weight, of the material to the product, such as the combustible fuel.
  • In another aspect, the invention features methods of making a product, such as a combustible fuel that include providing a material that includes a carbohydrate produced by pretreating a biomass feedstock with any one or more of radiation, sonication, oxidation, pyrolysis, and steam explosion, wherein less than about 25 percent by weight of the biomass is hydrolyzed subsequent to pretreatment; and contacting the material with a microorganism having the ability to convert at least a portion of the material, e.g., at least about 1 percent by weight, to the product, such as the combustible fuel.
  • In another aspect, the invention features methods of making a product, such as a combustible fuel, that includes providing a material includes a carbohydrate produced by pretreating a biomass feedstock with any one or more of radiation, sonication, oxidation, pyrolysis, and steam explosion, in which less than about 25 percent by weight of the biomass is in contact with a liquid, such as water, and contacting the material with a microorganism having the ability to convert at least a portion, e.g., at least about 1 percent by weight, of the material to the product, such as the combustible fuel.
  • In some embodiments, the methods include selecting two or more different pretreatment methods. The example, the two or more different pretreatment methods can include radiation and sonication, radiation and oxidation, radiation and pyrolization, sonication and oxidation, sonication and pyrolization, or oxidation and pyrolization. Optionally, pretreating the biomass can include steam explosion.
  • In another aspect, the invention features methods of making a product, such as a combustible fuel, that include providing a material comprising a carbohydrate produced by pretreating a sheared biomass feedstock with any one or more of radiation, sonication, oxidation, pyrolysis, and steam explosion; and contacting the material with a microorganism having the ability to convert at least a portion, e.g., at least about 1 percent by weight, of the material to the product, such as the combustible fuel.
  • For example, the sheared biomass can include discrete fibers having a length-to-diameter ratio (L/D) of greater than about 5/1. For example, the biomass can have internal fibers, and the biomass has been sheared to an extent that its internal fibers are substantially exposed. For example, the biomass has been sheared to an extent that it has a bulk density of less than about 0.35 g/cm3.
  • In another aspect, the invention features biomass feedstock processing systems tat include a biomass feedstock preparation module for reducing size of pieces of biomass; two or more of the following pretreatment modules: a radiation module arranged to apply radiation to the biomass; a sonication module arranged to apply sonic energy to the biomass; an oxidation module arranged to oxidize the biomass; a pyrolysis module arranged to apply heat to the biomass; and a biomass transportation subsystem to move the biomass to and between modules within the processing system. The two or more pretreatment modules are arranged in series and/or are arranged to treat a portion of the biomass at about the same time. For example, any system can further include a vessel.
  • In another aspect, the invention features systems that include a reaction vessel containing a pretreated biomass material that includes a carbohydrate. The pretreated biomass material is produced by any method described herein.
  • For example, the vessel can also contains a microorganism in contact with the material, the microorganism having the ability to convert at least a portion of the material to a product, such as a combustible fuel. For example, the vessel can have a total volume of greater than about 1,000 L, such as greater than 5,000 L.
  • For example, any system can include a radiation module and a sonication module.
  • In another aspect, the invention features carbohydrate materials produced by a process that includes pretreating a sheared biomass feedstock with any one or more of radiation, sonication, oxidation, pyrolysis and steam explosion. For example, pretreating can be performed with any two or more of radiation, sonication, oxidation, pyrolysis, and steam explosion.
  • In another aspect, the invention features carbohydrate materials produced by a process that includes pretreating a biomass feedstock with any two or more of radiation, sonication, oxidation, pyrolysis, and steam explosion.
  • In another aspect, the invention features compositions that include a cellulosic or a lignocellulosic material having a peak maximum molecular weight of less than about 25,000, and a crystallinity of less than about 55 percent. For example, the cellulosic or a lignocellulosic material can have a porosity of greater than about 72 percent, a BET surface greater than about 0.75 m2/g, or a bulk density of less than about 0.5 g/cm3. For example, the composition can further include an enzyme and/or a microbe.
  • In another aspect, the invention features compositions that include a cellulosic or a lignocellulosic material that includes fibers. The cellulosic or lignocellulosic material has a peak maximum molecular weight of less than about 25,000, and a bulk density of less than about 0.5 g/cm3.
  • In another aspect, the invention features methods of making composites, such as a fiber-resin composite that include irradiating a fibrous material that includes a first cellulosic and/or lignocellulosic material having a first molecular weight to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight; and combining the second cellulosic and/or lignocellulosic material with a material, such as a resin.
  • In another aspect, the invention features methods of making composites, such as a fiber-resin composite, that include combining a material, such as a resin, with a fibrous material that includes a cellulosic and/or lignocellulosic material having a first molecular weight to provide a composite that includes the fibrous material and a matrix; and irradiating the composite to increase molecular weight of the first cellulosic and/or lignocellulosic material within the matrix, such as a resin matrix.
  • In another aspect, the invention features methods of making composites, such as a fiber-resin composites that include irradiating a fibrous material that includes a first cellulosic and/or lignocellulosic material having a first molecular weight to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight; combining the second cellulosic and/or lignocellulosic material with a material, such as a resin, to provide a composite; and irradiating the composite.
  • In another aspect, the invention features methods of making irradiated wood products that include providing a wood product that includes a first carbohydrate-containing material having a first molecular weight; and irradiating the wood product to provide an irradiated wood product that includes a second carbohydrate-containing material having a second molecular weight higher than the first molecular weight. For example, the methods can further include sonicating, e.g., prior to, after, or concurrently with the irradiating.
  • Methods are disclosed that include providing a first material that includes cellulose having a first number average molecular weight; irradiating the first material to provide a second material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight; and combining the second material with a microorganism. The microorganism utilizes, e.g., ferments or otherwise converts, the second material, and in some instances the first material, to produce a useful material, e.g., a combustible fuel. For example, the combustible fuel can include one or more of hydrogen, an alcohol, an organic acid, a hydrocarbon or mixtures of these. A preferred material is ethanol or butanol, e.g., n-, sec- or t-butanol.
  • In some embodiments, the first material includes a cellulosic or a lignocellulosic material. For example, the first material can be or can include paper, paper products, wood, wood-related materials, particle board, grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, rice hulls, algae, seaweed, coconut hair, cotton, synthetic celluloses or mixtures of any of these materials.
  • In preferred embodiments, the first material is in the form of a fibrous material that includes fibers provided by shearing a fiber source. Shearing alone can reduce the crystallinity of a fibrous material and can work synergistically with any process technique that also reduces crystallinity and/or molecular weight. For example, the shearing can be performed with a rotary knife cutter. In some embodiments, the fibrous material has an average length-to-diameter ratio of greater than 5/1.
  • The first and/or second material can have, e.g., a BET surface area of greater than 0.25 m2/g and/or a porosity of greater than about 25 percent.
  • In some embodiments, the irradiating is performed with an ionizing radiation, such as gamma rays or a beam of electrons.
  • In preferred embodiments, the microorganism is a bacterium or a fungus, such as a yeast.
  • In some embodiments, the second number average molecular weight is at least about 25 percent lower than the first number average molecular weight, e.g., 50 percent lower.
  • Methods are disclosed that include shearing a fiber source to provide a first fibrous material that includes cellulose having a first number average molecular weight; and irradiating the first fibrous material to provide a second fibrous material that includes a cellulose having a second number average molecular weight lower that the first number average molecular weight. Shearing can work synergistically with radiation to reduce crystallinity and/or molecular weight.
  • Such methods may further include combining the second material with a microorganism.
  • Methods are disclosed that include irradiating a fiber source, e.g., a paper, that includes cellulose having a first number average molecular weight to provide an irradiated fiber source that includes cellulose having a second number average molecular weight less than the first number average molecular weight; and shearing the irradiated fiber source to provide a fibrous material. Relative to the pre-irradiated material, the irradiated material can be brittle and more susceptible to "opening up" during the shearing.
  • Such methods can further include combining the fibrous material with a microorganism.
  • Methods are disclosed that include providing a first lignocellulosic material that includes cellulose having a first number average molecular weight; and irradiating the first lignocellulosic material to provide a second lignocellulosic material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight.
  • Such methods can further include combining the second lignocellulosic material with a microorganism or removing lignin from the second lignocellulosic material to provide a de-lignified material, and then combining the de-lignified material with a microorganism the microorganism. For example, the lignin from the processing can be utilized as a processing aid for plastics or it can be burned to produce energy.
  • Methods are disclosed that include providing a first fibrous material that includes cellulose having a first number average molecular weight; densifying the first fibrous material to provide a densified first fibrous material; and irradiating the densified first fibrous material to provide a densified second material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight. Densification, can work synergistically with irradiation to lower molecular weight and can also increase throughput in any processing step described herein.
  • Such methods can further include combining the second densified fibrous material with a microorganism or fiberizing the second densifed fibrous material to provide a second fibrous material, and then combining the second fibrous material with a microorganism.
  • To further aid in the reduction of the molecular weight of the cellulose, an enzyme, e.g., a cellulolytic enzyme and/or a swelling agent, can be utilized with any method described herein.
  • Methods are disclosed that include sonicating a first material that includes cellulose having a first number average molecular weight to provide a second material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight; and combining the second material with a microorganism. The microorganism utilizes, e.g., ferments or otherwise converts, the second material, and in some instances the first material, to produce a useful material, e.g., a combustible fuel. For example, the combustible fuel can be or can include hydrogen, an alcohol, an organic acid, a hydrocarbon or mixtures of these. A preferred material is ethanol or butanol, e.g., n-, sec- to t-butanol.
  • In some embodiments, the first material includes a cellulosic or a lignocellulosic material. For example, the first material can be or can include paper, paper products, wood, wood-related materials, particle board, grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, rice hulls, algae, seaweed, coconut hair, cotton, synthetic celluloses or mixtures of any of these materials.
  • In preferred embodiments, the first material is in the form of a fibrous material that includes fibers provided by shearing a fiber source. Shearing can work synergistically with sonication to reduce molecular weight and/or crystallinity. For example, the shearing can be performed with a rotary knife cutter. In some embodiments, the fibrous material has an average length-to-diameter ratio of greater than 5/1.
  • The first and/or second material can have, e.g., a BET surface area of greater than 0.25 m2/g and/or a porosity of greater than about 25 percent.
  • In some embodiments, the sonicating is performed with sound having a frequency of from about 16 kHz to about 100 kHz and/or an intensity of from about 30 W/cm2 to about 600 W/cm2.
  • In preferred embodiments, the microorganism is a bacterium or a fungus, such as a yeast.
  • In some embodiments, the second number average molecular weight is at least about 25 percent lower than the first number average molecular weight, e.g., 50 percent lower.
  • Methods are disclosed that include shearing a fiber source to provide a first fibrous material that includes cellulose having a first number average molecular weight; and sonicating the first fibrous material to provide a second fibrous material that includes a cellulose having a second number average molecular weight lower that the first number average molecular weight.
  • Such methods may further include combining the second material with a microorganism.
  • Methods are disclosed that include sonicating a fiber source, e.g., a paper, that includes cellulose having a first number average molecular weight to provide a sonicated fiber source that includes cellulose having a second number average molecular weight less than the first number average molecular weight; and shearing the sonicated fiber source to provide a fibrous material. Relative to the pre-sonicated material, the sonicated material can be brittle and more susceptible to "opening up" during the shearing.
  • Such methods can further include combining the fibrous material with a microorganism.
  • Methods are disclosed that include sonicating a first lignocellulosic material that includes cellulose having a first number average molecular weight to provide a second lignocellulosic material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight.
  • Such methods can further include combining the second lignocellulosic material with a microorganism or removing lignin from the second lignocellulosic material to provide a de-lignified material, and then combining the de-lignified material with a microorganism the microorganism.
  • Methods are disclosed that include sonicating a first fibrous material that includes cellulose having a first number average molecular weight to provide a second fibrous material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight; and densifying the second fibrous material to provide a densified fibrous material.
  • Such methods can further include combining the densified fibrous material with a microorganism or fiberizing the densified fibrous material to provide a third fibrous material, and then combining the third fibrous material with a microorganism.
  • To further aid in the reduction of the molecular weight of the cellulose, an enzyme, e.g., a cellulolytic enzyme, or a chemical, e.g., sodium hypochlorite, an acid, a base or a swelling agent, can be utilized with any method described herein. The enzyme and/or chemical treatment can occur before, during or after sonication.
  • Methods are disclosed that include pyrolyzing a first material that includes cellulose having a first number average molecular weight to provide a second material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight; and combining the second material with a microorganism. The microorganism utilizes, e.g., ferments or otherwise converts, the second material, and in some instances the first material, to produce a useful material, e.g., a combustible fuel. For example, the combustible fuel can include one or more of hydrogen, an alcohol, an organic acid, a hydrocarbon or mixtures of these. A preferred material is ethanol or butanol.
  • In some embodiments, the first material includes a cellulosic or a lignocellulosic material. For example, the first material can be or can include paper, paper products, wood, wood-related materials, particle board, grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, rice hulls, algae, seaweed, coconut hair, cotton, synthetic celluloses or mixtures of any of these materials.
  • In preferred embodiments, the first material is in the form of a fibrous material that includes fibers provided by shearing a fiber source. Relatively small cross-section can often be pyrolyzed with greater control and efficiency. For example, the shearing can be performed with a rotary knife cutter. In some embodiments, the fibrous material has an average length-to-diameter ratio of greater than 5/1.
  • The first and/or second material can have, e.g., a BET surface area of greater than 0.25 m2/g and/or a porosity of greater than about 25 percent. High surface areas and/or porosities can enhance reaction rates, making processes more efficient.
  • In preferred embodiments, the microorganism is a bacterium or a fungus, such as a yeast.
  • In some embodiments, the second number average molecular weight is at least about 25 percent lower than the first number average molecular weight, e.g., 50 percent lower.
  • Methods are disclosed that include shearing a fiber source to provide a first fibrous material that includes cellulose having a first number average molecular weight; and pyrolyzing the first fibrous material to provide a second fibrous material that includes a cellulose having a second number average molecular weight lower that the first number average molecular weight.
  • Such methods may further include combining the second material with a microorganism.
  • Methods that include pyrolyzing a fiber source, e.g., a paper, that includes cellulose having a first number average molecular weight to provide a pyrolyzed fiber source that includes cellulose having a second number average molecular weight less than the first number average molecular weight; and shearing the pyrolyzed fiber source to provide a fibrous material. Relative to the pre-pyrolyzed material, the pyrolyzed material can be brittle and more susceptible to "opening up" during the shearing. Shearing pyrolyzed material can be less energy intensive and can be more efficient.
  • Such methods can further include combining the fibrous material with a microorganism.
  • Methods are disclosed that include pyrolyzing a first lignocellulosic material that includes cellulose having a first number average molecular weight to provide a second lignocellulosic material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight.
  • Such methods can further include combining the second lignocellulosic material with a microorganism or removing lignin from the second lignocellulosic material to provide a de-lignified material, and then combining the de-lignified material with a microorganism the microorganism.
  • Methods are disclosed that include pyrolyzing a first fibrous material that includes cellulose having a first number average molecular weight to provide a second fibrous material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight; and densifying the second fibrous material to provide a densified fibrous material.
  • Such methods can further include combining the densified fibrous material with a microorganism or fiberizing the densified fibrous material to provide a third fibrous material, and then combining the third fibrous material with a microorganism.
  • To further aid in the reduction of the molecular weight of the cellulose, an enzyme, e.g., a cellulolytic enzyme, or a chemical, e.g., sodium hypochlorite or an acid or base, can be utilized with any method described herein. The enzyme and/or chemical treatment can occur before, during or after pyrolyzing.
  • In any aspect or embodiment described herein, pyrolyzing may include any one or more of the following features. The pyrolyzing can include heating the first material using a resistive heating member, such as a metal filament or metal ribbon. The heating can occur by direct contact between the resistive heating member and the first material. The pyrolyzing can include heating the first material by induction, such as by using a Currie-Point pyrolyzer. The pyrolyzing can include heating the first material by the application of radiation, such as infrared radiation. The radiation can be generated by a laser, such as an infrared laser. The pyrolyzing can include heating the first material with a convective heat. The convective heat can be generated by a flowing stream of heated gas. The heated gas can be maintained at a temperature of less than about 1200 °C, such as less than 1000 °C, less than 750 °C, less than 600 °C, less than 400 °C or even less than 300 °C. The heated gas can be maintained at a temperature of greater than about 250 °C. The convective heat can be generated by a hot body surrounding the first material, such as in a furnace. The pyrolyzing can include heating the first material with steam at a temperature above about 250 °C.
  • Methods are disclosed that include oxidizing a first material that includes cellulose having a first number average molecular weight and having a first oxygen content to provide a second material that includes cellulose having a second number average molecular weight and having a second oxygen content higher than the first oxygen content. The second material can be combined with a resin, e.g., a molten thermoplastic resin, to provide a composite. A higher level of oxidation, while maintaining molecular weight, can provide composites with exceptional mechanical properties, such as improved abrasion resistance, compression strength, fracture resistance, impact strength, bending strength, tensile modulus, flexural modulus and elongation at break. The second material can also be combined with any solid and/or liquid described herein, or any solid and/or liquid described in any patent application, patent or publication incorporated by reference herein.
  • To further improve dispersability, the resin can include a component that includes hydrogen-bonding groups, such as one or more anhydride groups, carboxylic acid groups, hydroxyl groups, amide groups, amine groups or mixtures of any of these groups. In some preferred embodiments, the component includes a polymer copolymerized with and/or grafted with maleic anhydride. Such materials are available from Dupont under the tradename FUSABOND®.
  • The first material can be or can include, e.g., paper, paper products, wood, wood-related materials, particle board, grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, rice hulls, coconut hair, cotton, synthetic celluloses or mixtures of any of these materials. Other materials that include cellulose are described herein. Still other materials that include cellulose are described in the patents, patent applications and publications that have been incorporated by reference herein.
  • In some desirable embodiments, the first material is in the form of a fibrous material that includes fibers. Such fibrous materials can be, e.g., provided by shearing a fiber source, such as by shearing a fiber source using a rotary knife cutter. For example, to maximize mechanical properties, it is often desirable that the fibers of the fibrous material have an average length-to-diameter ratio of greater than 5/1. For example, to maximize dispersability, it is often desirable that the first and/or second material have a BET surface area of greater than 0.25 m2/g and/or a porosity of greater than about 25 percent.
  • Oxidation of the materials described herein can be aided by a variety of techniques, including pyrolysis. For example, the oxidizing can include pyrolyzing the first material by heating the first material using a resistive heating member, such as a metal filament or metal ribbon, in a oxidizing environment, such as in the presence of air, an oxygen-enriched inert gas (e.g., argon), or oxygen itself. In some preferred methods, the heating occurs by direct contact between the resistive heating member and the first material. In other methods, oxidizing includes pyrolyzing the first material by heating the first material by induction, such as by a Currie-Point pyrolyzer, in an oxidizing environment. In other methods, oxidizing includes pyrolyzing the first material by heating the first material by the application of radiation, such as infrared radiation, in an oxidizing environment. In one method, the radiation is generated by an infrared laser. In still other methods, oxidizing includes pyrolyzing the first material by heating the first material with a convective heat in an oxidizing environment. For example, the convective heat can be generated by a flowing stream of heated gas. For example, the heated gas can be maintained at a temperature of less than about 1200 °C, such as less than 1000 °C, less than 750 °C, less than 600 °C, less than 400 °C or even less than 300 °C. In other methods, the convective heat is generated by a hot body surrounding the first material. In yet other methods, the oxidizing includes pyrolyzing the first material by heating the first material with steam at a temperature above about 250 °C.
  • Oxidation of the materials can be aided by still other techniques, including sonication. For example, the oxidizing can include sonicating the first material in an oxidizing environment. For example, the sonication can be performed while the first material is dispersed in an aqueous medium. In some desirable embodiments, the sonication is performed using sound having a frequency of from about 12 kHz to about 25 kHz.
  • Oxidation of the materials can be performed by still other techniques, including ionizing and/or non-ionizing radiation. For example, the oxidizing can include irradiating the first material with gamma rays in an oxidizing environment and/or irradiating the first material with a beam of electrons in an oxidizing environment.
  • In some desirable embodiments for providing composites, the second number average molecular weight is not more than fifteen percent lower than the first number average molecular weight. In some embodiments for providing composites, the second number average molecular weight is substantially the same as the first number average molecular weight.
  • In some desirable embodiments, the second oxygen content is at least about five percent higher than the first oxygen content, or even more preferably, twenty percent higher than the first oxygen content.
  • Methods are disclosed that include shearing a fiber source to provide a first fibrous material that includes cellulose having a first number average molecular weight and having a first oxygen content. The first fibrous material is oxidized to provide a second fibrous material that includes cellulose having a second number average molecular weight and having a second oxygen content higher than the first oxygen content. The second fibrous material can be utilized to make composites or it can be utilized for other applications. For example, the second material can be combined with any solid and/or liquid described herein, or any solid and/or liquid described in any patent application, patent or publication incorporated by reference herein.
  • If desired, and when making a composite, the methods can further include combining the second fibrous material with a resin, such as a thermoplastic or thermosetting resin.
  • Methods are disclosed that include oxidizing a fiber source that includes cellulose having a first number average molecular weight and having a first oxygen content to provide an oxidized fiber source that includes cellulose having a second number average molecular weight and having a second oxygen content higher than the first oxygen content. The oxidized fiber source is then sheared to provide an oxidized fibrous material that includes fibers. The oxidized fibrous material can be utilized to make composites or it can be utilized for other applications. For example, the second material can be combined with any solid and/or liquid described herein, or any solid and/or liquid described in any patent application, patent or publication incorporated by reference herein.
  • Methods are disclosed that include oxidizing a first material that includes cellulose having a first number average molecular weight and having a first oxygen content to provide a second material that includes cellulose having a second number average molecular weight and having a second oxygen content higher than the first oxygen content. The second fibrous material is densified to provide a densified fibrous material.
  • If desired, these methods can further include combining the densified fibrous material with a resin. In some preferred embodiment, the methods further include fiberization of the densified fibrous material to provide a third fibrous material, and then combining the third fibrous material with a resin, such as a thermoplastic resin. The densified or third fibrous material can be also combined with any solid and/or liquid described herein, or any solid and/or liquid described in any patent application, patent or publication incorporated by reference herein.
  • Methods are disclosed that include converting a first material that includes cellulose having a first number average molecular weight and having a first oxygen content to a second material that includes cellulose having a second number average molecular weight and having a second oxygen content higher than the first oxygen content; and combining the second material with a resin to provide a composite material. The first and/or second material can also be combined with any solid and/or liquid described herein, or any solid and/or liquid described in any patent application, patent or publication incorporated by reference herein.
  • Methods are disclosed that include oxidizing a first material that includes cellulose having a first number average molecular weight and having a first oxygen content to provide a second material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight and having a second oxygen content higher than the first oxygen content; and combining the second material with a microorganism. The microorganism can utilize the second material, e.g., by fermentation, to produce a fuel, such as hydrogen, alcohols, organic acids and hydrocarbons or mixtures of any of these fuels. In some embodiments, the first material is combined as well.
  • Methods are disclosed that include converting a first material that includes cellulose having a first number average molecular weight and having a first oxygen content to a second material that includes cellulose having a second number average molecular weight lower than the first number average molecular weight and having a second oxygen content higher than the first oxygen content; and combining the second material with a solid and/or a liquid, such as a liquid that includes a microorganism, and/or an enzyme. In some instances, the first material is combined as well. In some instances, the microorganism utilizes the second material to produce a fuel, such as hydrogen, alcohols, organic acids and hydrocarbons or mixtures of any of these fuels. In some embodiments, the first material can also be utilized by the microorganism to produce a fuel.
  • When a microorganism is utilized, it can be a natural microorganism or an engineered microorganism. For example, the microorganism can be a bacterium, e.g., a cellulolytic bacterium, a fungus, e.g., a yeast, a plant or a protist, e.g., an algae, a protozoa or a fungus-like protist, e.g., a slime mold. When the organisms are compatible, mixtures may be utilized. Generally, various microorganisms can produce a number of useful products, such as a fuel, by operating on, e.g., fermenting the materials. For example, alcohols, organic acids, hydrocarbons, hydrogen, proteins or mixtures of any of these materials can be produced by fermentation or other processes.
  • Methods are disclosed that include shearing and steam exploding a fiber source to form a fibrous material; and contacting the fibrous material with a microorganism to produce a product. Examples of useful products include hydrogen, alcohols, organic acids, hydrocarbons, proteins, and combinations thereof. Examples of useful fiber sources include cellulosic material, lignocellulosic material, and combinations thereof.
  • Shearing and steam exploding the fiber source to form the fibrous material may be performed in any order. In addition, multiple shearing and/or steam exploding operations may be performed in any order. Shearing may be performed, for example, using a rotary knife cutter. The fiber source may be cut prior to shearing and/or steam exploding.
  • For example, in some embodiments, the method includes shearing the fiber source to form a sheared fiber source, and then steam exploding the sheared fiber source to form the fibrous material. It is also possible to produce fibrous material by additionally shearing the steam exploded, sheared fiber source. It is also possible to shear the fiber source a second time to produce a second sheared fiber source, which is then steam exploded to produce the fibrous material.
  • Methods are disclosed that include steam exploding the fiber source to form a steam exploded fiber source, and then shearing the steam exploded fiber source to produce the fibrous material. It is also possible to produce fibrous material by additionally steam exploding the sheared, steam exploded fiber source.
  • Methods are disclosed that include shearing and steam exploding the fiber source concurrently to produce the fibrous material.
  • In some embodiments, the method may include passing sheared material through one or more screens, e.g., a screen having an average opening size of 1.59 mm or less (0.0625 inch). Screening separates the material according to size. For example, in one embodiment, the method includes: shearing the fiber source to produce a sheared fiber source; passing the sheared fiber source through a first screen to produce a screened fiber source; shearing the screened fiber source to produce a second sheared fiber source; passing the second sheared fiber source through a second screen having an average opening size less than the first screen to provide a second screened fiber source; and steam exploding the second screened fiber source to produce the fibrous material. The method may further include shearing the second screened fiber source to produce a third sheared fiber source, and then steam exploding the third sheared fibers source to produce the fibrous material.
  • It is also possible to shear the fiber source and concurrently pass it through a screen.
  • The methods may also further include encapsulating the fibrous material in a substantially gas impermeable material to remove entrapped gas and densify the fibrous material. The substantially gas impermeable material may be soluble in water, and may be provided in the form of a bag.
  • Examples of microorganisms that may be used to produce the useful product include bacteria, yeasts, enzymes, or combinations thereof. For example, the microorganism can be a bacterium, e.g., a cellulolytic bacterium, a fungus, e.g., a yeast, a plant or a protist, e.g., an algae, a protozoa or a fungus-like protist, e.g., a slime mold.
  • Examples of products that may be produced include mono- and polyfunctional C1-C6 alkyl alcohols, mono- and poly-functional carboxylic acids, C1-C6 hydrocarbons, and combinations thereof. Specific examples of suitable alcohols include methanol, ethanol, propanol, isopropanol, butanol, ethylene glycol, propylene glycol, 1,4-butane diol, glycerin, and combinations thereof. Specific example of suitable carboxylic acids include formic acid, acetic acid, propionic acid, butyric acid, valeric acid, caproic acid, palmitic acid, stearic acid, oxalic acid, malonic acid, succinic acid, glutaric acid, oleic acid, linoleic acid, glycolic acid, lactic acid, γ-hydroxybutyric acid, and combinations thereof. Examples of suitable hydrocarbons include methane, ethane, propane, pentane, n-hexane, and combinations thereof. Many of these products may be used as fuels.
  • Examples of microorganisms that may be used to produce useful products include bacteria, yeasts, or combinations thereof. For example, the microorganism can be a bacterium, e.g., a cellulolytic bacterium, a fungus, e.g., a yeast, a plant or a protist, e.g., an algae, a protozoa or a fungus-like protist, e.g., a slime mold.
  • Examples of products that may be produced include mono- and polyfunctional C1-C6 alkyl alcohols, mono- and poly-functional carboxylic acids, C1-C6 hydrocarbons, and combinations thereof. Specific examples of suitable alcohols include methanol, ethanol, propanol, isopropanol, butanol, ethylene glycol, propylene glycol, 1,4-butane diol, glycerin, and combinations thereof. Specific example of suitable carboxylic acids include formic acid, acetic acid, propionic acid, butyric acid, valeric acid, caproic acid, palmitic acid, stearic acid, oxalic acid, malonic acid, succinic acid, glutaric acid, oleic acid, linoleic acid, glycolic acid, lactic acid, γ-hydroxybutyric acid, and combinations thereof. Examples of suitable hydrocarbons include methane, ethane, propane, pentane, n-hexane, and combinations thereof. Many of these products may be used as fuels.
  • The term "fibrous material," as used herein, is a material that includes numerous loose, discrete and separable fibers. For example, a fibrous material can be prepared from a bleached Kraft paper fiber source by shearing, e.g., with a rotary knife cutter.
  • The term "screen," as used herein, means a member capable of sieving material according to size. Examples of screens include a perforated plate, cylinder or the like, or a wire mesh or cloth fabric.
  • The term "pyrolysis," as used herein, means to break bonds in a material by the application of heat energy. Pyrolysis can occur while the subject material is under vacuum, or immersed in a gaseous material, such as an oxidizing gas, e.g., air or oxygen, or a reducing gas, such as hydrogen.
  • Oxygen content is measured by elemental analysis by pyrolyzing a sample in a furnace operating at 1300 °C or above.
  • The terms "biomass" refers to any non-fossilized, i.e., renewable, organic matter. The various types of biomass include plant biomass (defined below), animal biomass (any animal by-product, animal waste, etc.) and municipal waste biomass (residential and light commercial refuse with recyclables such as metal and glass removed).
  • The term "plant biomass" and "lingocellulosic biomass" refer to virtually any plant-derived organic matter (woody or non-woody) available for energy on a sustainable basis. Plant biomass can include, but is not limited to, agricultural crop wastes and residues such as corn stover, wheat straw, rice straw, sugar cane bagasse, and the like. Plant biomass further includes, but is not limited to, trees, woody energy crops, wood wastes and residues such as softwood forest thinnings, barky wastes, sawdust, paper and pulp industry waste streams, wood fiber, and the like. Additionally grass crops, such as switchgrass and the like have potential to be produced on a large-scale as another plant biomass source. For urban areas, the best potential plant biomass feedstock includes yard waste (e.g., grass clippings, leaves; tree clippings, and brush) and vegetable processing waste. "Lignocellulosic feedstock," is any type of plant biomass such as, but not limited to, non-woody plant biomass, cultivated crops, such as, but not limited to, grasses, for example, but not limited to, C4 grasses, such as switchgrass, cord grass, rye grass, miscanthus, reed canary grass, or a combination thereof, or sugar processing residues such as bagasse, or beet pulp, agricultural residues, for example, soybean stover, corn stover, rice straw, rice hulls, barley straw, corn cobs, wheat straw, canola straw, rice straw, oat straw, oat hulls, corn fiber, recycled wood pulp fiber, sawdust, hardwood, for example aspen wood and sawdust, softwood, or a combination thereof. Further, the lignocellulosic feedstock may include cellulosic waste material such as, but not limited to, newsprint, cardboard, sawdust, and the like.
  • Lignocellulosic feedstock may include one species of fiber or alternatively, lignocellulosic feedstock may include a mixture of fibers that originate from different lignocellulosic feedstocks. Furthermore, the lignocellulosic feedstock may comprise fresh lignocellulosic feedstock, partially dried lignocellulosic feedstock, fully dried lignocellulosic feedstock or a combination thereof.
  • For the purposes of this disclosure, carbohydrates are materials that are composed entirely of one or more saccharide units or that include one or more saccharide units. Carbohydrates can be polymeric (e.g., equal to or greater than 10-mer, 100-mer, 1,000-mer, 10,000-mer, or 100,000-mer), oligomeric (e.g., equal to or greater than a 4-mer, 5-mer, 6-mer, 7-mer, 9-mer, 9-mer or 10-mer), trimeric, dimeric, or monomeric. When the carbohydrates are formed of more than a single repeat unit, each repeat unit can be the same or different.
  • Examples of polymeric carbohydrates include cellulose, xylan, pectin, and starch, while cellobiose and lactose are examples of dimeric carbohydrates. Examples of monomeric carbohydrates include glucose and xylose.
  • Carbohydrates can be part of a supramolecular structure, e.g., covalently bonded into the structure. Examples of such materials include lignocellulosic materials, such as that found in wood.
  • A combustible fuel is a material capable of burning in the presence of oxygen. Examples of combustible fuels include ethanol, n-propanol, n-butanol, hydrogen and mixtures of any two or more of these.
  • Swelling agents as used herein are materials that cause a discernable swelling, e.g., a 2.5 percent increase in volume over an unswollen state of cellulosic and/or lignocellulosic materials, when applied to such materials as a solution, e.g., a water solution. Examples include alkaline substances, such as sodium hydroxide, potassium hydroxide, lithium hydroxide and ammonium hydroxides, acidifying agents, such as mineral acids (e.g., sulfuric acid, hydrochloric acid and phosphoric acid), salts, such as zinc chloride, calcium carbonate, sodium carbonate, benzyltrimethylammonium sulfate, and basic organic amines, such as ethylene diamine.
  • A "sheared material," as used herein, is a material that includes discrete fibers in which at least about 50% of the discrete fibers, have a length/diameter (L/D) ratio of at least about 5, and that has an uncompressed bulk density of less than about 0.6 g/cm3. A sheared material is thus different from a material that has been cut, chopped or ground.
  • Changing a molecular structure of a biomass feedstock, as used herein, means to change the chemical bonding arrangement or conformation of the structure. For example, the change in the molecular structure can include changing the supramolecular structure of the material, oxidation of the material, changing an average molecular weight, changing an average crystallinity, changing a surface area, changing a degree of polymerization, changing a porosity, changing a degree of branching, grafting on other materials, changing a crystalline domain size, or an changing an overall domain size.
  • Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. Although methods and materials similar or equivalent to those described herein can be used in the practice or testing of the present invention, suitable methods and materials are described below. All publications, patent applications, patents, and other references mentioned herein are incorporated by reference in their entirety In case of conflict, the present specification, including definitions, will control. In addition, the materials, methods, and examples are illustrative only and not intended to be limiting.
  • Other features and advantages of the invention will be apparent from the following detailed description, and from the claims.
  • DESCRIPTION OF DRAWINGS
    • FIG. 1 is a block diagram illustrating conversion of biomass into products and co-products.
    • FIG. 2 is block diagram illustrating conversion of a fiber source into a first and second fibrous material.
    • FIG. 3 is a cross-sectional view of a rotary knife cutter.
    • FIG. 4 is block diagram illustrating conversion of a fiber source into a first, second and third fibrous material.
    • FIG. 5 is block diagram illustrating densification of a material.
    • FIG. 6 is a perspective view of a pellet mill.
    • FIG. 7A is a densified fibrous material in pellet form.
    • FIG. 7B is a transverse cross-section of a hollow pellet in which a center of the hollow is in-line with a center of the pellet.
    • FIG. 7C is a transverse cross-section of a hollow pellet in which a center of the hollow is out of line with the center of the pellet.
    • FIG. 7D is a transverse cross-section of a tri-lobal pellet.
    • FIG. 8 is a block diagram illustrating a treatment sequence for processing feedstock.
    • FIG. 9 is a perspective, cut-away view of a gamma irradiator.
    • FIG. 10 is an enlarged perspective view of region R of FIG. 9.
    • FIG. 11 is a block diagram illustrating an electron beam irradiation feedstock pretreatment sequence.
    • FIG. 12 is a schematic view of a system for sonicating a process stream of cellulosic material in a liquid medium.
    • FIG. 13 is a schematic view of a sonicator having two transducers coupled to a single horn.
    • FIG. 14 is a block diagram illustrating a pyrolytic feedstock pretreatment system.
    • FIG. 15 is a cross-sectional side view of a pyrolysis chamber.
    • FIG. 16 is a cross-sectional side view of a pyrolysis chamber.
    • FIG. 17 is a cross-sectional side view of a pyrolyzer that includes a heated filament.
    • FIG. 18 is a schematic cross-sectional side view of a Curie-Point pyrolyzer.
    • FIG. 19 is a schematic cross-sectional side view of a furnace pyrolyzer.
    • FIG. 20 is a schematic cross-sectional top view of a laser pyrolysis apparatus.
    • FIG. 21 is a schematic cross-sectional top view of a tungsten filament flash pyrolyzer.
    • FIG. 22 is a block diagram illustrating an oxidative feedstock pretreatment system.
    • FIG. 23 is block diagram illustrating a general overview of the process of converting a fiber source into a product, e.g., ethanol.
    • FIG. 24 is a cross-sectional view of a steam explosion apparatus.
    • FIG. 25 is a schematic cross-sectional side view of a hybrid electron beam/sonication device.
    • FIG. 26 is a scanning electron micrograph of a fibrous material produced from polycoated paper at 25 X magnification. The fibrous material was produced on a rotary knife cutter utilizing a screen with 1/8 inch openings.
    • FIG. 27 is a scanning electron micrograph of a fibrous material produced from bleached Kraft board paper at 25 X magnification. The fibrous material was produced on a rotary knife cutter utilizing a screen with 1/8 inch openings.
    • FIG. 28 is a scanning electron micrograph of a fibrous material produced from bleached Kraft board paper at 25 X magnification. The fibrous material was twice sheared on a rotary knife cutter utilizing a screen with 1/16 inch openings during each shearing.
    • FIG. 29 is a scanning electron micrograph of a fibrous material produced from bleached Kraft board paper at 25 X magnification. The fibrous material was thrice sheared on a rotary knife cutter. During the first shearing, a 1/8 inch screen was used; during the second shearing, a 1/16 inch screen was used, and during the third shearing a 1/32 inch screen was used.
    • FIG. 30 is a schematic side view of a sonication apparatus, while FIG. 31 is a cross-sectional view through the processing cell of FIG. 30.
    • FIG. 32 is a scanning electron micrograph at 1000 X magnification of a fibrous material produced from shearing switchgrass on a rotary knife cutter, and then passing the sheared material through a 1/32 inch screen.
    • FIGS. 33 and 34 are scanning electron micrographs of the fibrous material of FIG. 32 after irradiation with 10 Mrad and 100 Mrad gamma rays, respectively, at 1000 X magnification.
    • FIG. 35 is a scanning electron micrographs of the fibrous material of FIG. 32 after irradiation with 10 Mrad and sonication at 1000 X magnification.
    • FIG. 36 is a scanning election micrographs of the fibrous material of FIG. 32 after irradiation with 100 Mrad and sonication at 1000 X magnification.
    • FIG. 37 is an infrared spectrum of Kraft board paper sheared on a rotary knife cutter.
    • FIG. 38 is an infrared spectrum of the Kraft paper of FIG. 47 after irradiation with 100 Mrad of gamma radiation.
    • FIG. 39 is a schematic view of a process for biomass conversion.
    • FIG. 40 is schematic view of another process for biomass conversion.
    DETAILED DESCRIPTION
  • Biomass (e.g., plant biomass, animal biomass, and municipal waste biomass) can be processed to produce useful products such as fuels. Systems and processes are described below that can use as feedstock materials such as cellulosic and/or lignocellulosic materials that are readily available, but can be difficult to process, for example, by fermentation. Feedstock materials are first physically prepared for processing, often by size reduction of raw feedstock materials. Physically prepared feedstock can be pretreated or processed using one or more of radiation, sonication, oxidation, pyrolysis, and steam explosion. The various pretreatment systems and methods can be used in combinations of two, three, or even four of these technologies.
  • In some cases, to provide materials that include a carbohydrate, such as cellulose, that can be converted by a microorganism to a number of desirable products, such as a combustible fuels (e.g., ethanol, butanol or hydrogen), feedstocks that include one or more saccharide units can be treated by any one or more of the processes described herein. Other products and co-products that can be produced include, for example, human food, animal feed, pharmaceuticals, and nutriceuticals. A number of examples are presented that range from bench scale implementations of individual pretreatment methods to large scale biomass processing plants.
  • TYPES OF BIOMASS
  • Generally, any biomass material that is or includes carbohydrates composed entirely of one or more saccharide units or that include one or more saccharide units can be processed by any of the methods described herein. For example, the biomass material can be cellulosic or lignocellulosic materials.
  • For example, such materials can include paper, paper products, wood, wood-related materials, particle board, grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, rice hulls, coconut hair, algae, seaweed, cotton, synthetic celluloses, or mixtures of any of these.
  • Fiber sources include cellulosic fiber sources, including paper and paper products (e.g., polycoated paper and Kraft paper), and lignocellulosic fiber sources, including wood, and wood-related materials, e.g., particle board. Other suitable fiber sources include natural fiber sources, e.g., grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, rice hulls, coconut hair, fiber sources high in α-cellulose content, e.g., cotton; and synthetic fiber sources, e.g., extruded yam (oriented yarn or un-oriented yam). Natural or synthetic fiber sources can be obtained from virgin scrap textile materials, e.g., remnants or they can be post consumer waste, e.g., rags. When paper products are used as fiber sources, they can be virgin materials, e.g., scrap virgin materials, or they can be post-consumer waste. Aside from virgin raw materials, post-consumer, industrial (e.g., offal), and processing waste (e.g., effluent from paper processing) can also be used as fiber sources. Also, the fiber source can be obtained or derived from human (e.g., sewage), animal or plant wastes. Additional fiber sources have been described in U.S. Patent Nos. 6,448,307, 6,258,876, 6,207,729, 5,973,035 and 5,952,105.
  • In some embodiments, the carbohydrate is or includes a material having one or more β-1,4-linkages and having a number average molecular weight between about 3,000 and 50,000. Such a carbohydrate is or includes cellulose (I), which is derived from (β-glucose 1) through condensation of β(1→ 4)-glycosidic bonds. This linkage contrasts itself with that for α(1→ 4)-glycosidic bonds present in starch and other carbohydrates.
    Figure imgb0001
    Figure imgb0002
  • Blends of any of the above materials may also be used.
  • SYSTEMS FOR TREATING BIOMASS
  • FIG. 1 shows a system 100 for converting biomass, particularly biomass with significant cellulosic and lignocellulosic components, into useful products and co-products. System 100 includes a feed preparation subsystem 110, a pretreatment subsystem 114, a primary process subsystem 118, and a post-processing subsystem 122. Feed preparation subsystem 110 receives biomass in its raw form physically prepares the biomass for use as feedstock by downstream processes (e.g., reduces the size of and homogenizes the biomass), and stores the biomass both in its raw and feedstock forms. Biomass feedstock with significant cellulosic and lignocellulosic components can have a high average molecular weight and crystallinity that can make processing the feedstock into useful products (e.g., fermenting the feedstock to produce ethanol) difficult.
  • Pretreatment subsystem 114 receives feedstock from the feed preparation subsystem 110 and prepares the feedstock for use in primary production processes by, for example, reducing the average molecular weight and crystallinity of the feedstock. Primary process subsystem 118 receives pretreated feedstock from pretreatment subsystem 114 and produces useful products (e.g., ethanol, other alcohols, pharmaceuticals, and/or food products). In some cases, the output of primary process subsystem 118 is directly useful but, in other cases, requires further processing provided by post-processing subsystem 122. Post-processing subsystem 122 provides further processing to product streams from primary process system 118 which require it (e.g., distillation and denaturation of ethanol) as well as treatment for waste streams from the other subsystems. In some cases, the cuts of subsystems 114,118,122 can also be directly or indirectly useful as secondary products and/or in increasing the overall efficiency of system 100. For example, post-processing subsystem 122 can produce treated water to be recycled for use as process water in other subsystems and/or can produce burnable waste which can be used as fuel for boilers producing steam and/or electricity.
  • The optimum size for biomass conversion plants is affected by factors including economies of scale and the type and availability of biomass used as feedstock. Increasing plant size tends to increase economies of scale associated with plant processes. However, increasing plant size also tends to increase the costs (e.g., transportation costs) per unit of feedstock. Studies analyzing these factors suggest that the appropriate size for biomass conversion plants can range from 2000 to 10,000 dried tons of feedstock per day depending at least in part on the type of feedstock used. The type of feedstock can also impact plant storage requirements with plants designed primarily for processing feedstock whose availability varies seasonally (e.g., corn stower) requiring more on- or of-site feedstock storage than plants designed to process feedstock whose availability is relatively steady (e.g., waste paper).
  • FEED PREPARATION
  • In some cases, methods of processing begin with a physical preparation of the feedstock, e.g., size reduction of raw feedstock materials, such as by cutting, grinding, shearing or chopping. In some cases, loose feedstock (e.g., recycled paper or switchgrass) is prepared by shearing or shredding. Screens and/or magnets can be used to remove oversized or undesirable objects such as, for example, rocks or nails from the feed stream.
  • Feed preparation systems can be configured to produce feed streams with specific characteristics such as, for example, specific maximum sizes, specific length-to-width, or specific surface areas ratios. As a part of feed preparation, the bulk density of feedstocks can be controlled (e.g., increased).
  • Size Reduction
  • In some embodiments, the material to be processed is in the form of a fibrous material that includes fibers provided by shearing a fiber source. For example, the shearing can be performed with a rotary knife cutter.
  • For example, and by reference to FIG 2, a fiber source 210 is sheared, e.g., in a rotary knife cutter, to provide a first fibrous material 212. The first fibrous material 212 is passed through a first screen 214 having an average opening size of 1.59 mm or less (1/16 inch, 0.0625 inch) to provide a second fibrous material 216. If desired, fiber source can be cut prior to the shearing, e.g., with a shredder. For example, when a paper is used as the fiber source, the paper can be first cut into strips that are, e.g., 1/4- to 1/2-inch wide, using a shredder, e.g., a counter-rotating screw shredder, such as those manufactured by Munson (Utica, N.Y). As an alternative to shredding, the paper can be reduced in size by cutting to a desired size using a guillotine cutter. For example, the guillotine cutter can be used to cut the paper into sheets that are, e.g., 10 inches wide by 12 inches long.
  • In some embodiments, the shearing of fiber source and the passing of the resulting first fibrous material through first screen are performed concurrently. The shearing and the passing can also be performed in a batch-type process.
  • For example, a rotary knife cutter can be used to concurrently shear the fiber source and screen the first fibrous material. Referring to FIG 3, a rotary knife cutter 220 includes a hopper 222 that can be loaded with a shredded fiber source 224 prepared by shredding fiber source. Shredded fiber source is sheared between stationary blades 230 and rotating blades 232 to provide a first fibrous material 240. First fibrous material 240 passes through screen 242, and the resulting second fibrous material 244 is captured in bin 250. To aid in the collection of the second fibrous material, the bin can have a pressure below nominal atmospheric pressure, e.g., at least 10 percent below nominal atmospheric pressure, e.g., at least 25 percent below nominal atmospheric pressure, at least 50 percent below nominal atmospheric pressure, or at least 75 percent below nominal atmospheric pressure. In some embodiments, a vacuum source 252 is utilized to maintain the bin below nominal atmospheric pressure.
  • Shearing can be advantageous for "opening up" and "stressing" the fibrous materials, making the cellulose of the materials more susceptible to chain scission and/or reduction of crystallinity. The open materials can also be more susceptible to oxidation when irradiated.
  • The fiber source can be sheared in a dry state, a hydrated state (e.g., having up to ten percent by weight absorbed water), or in a wet state, e.g., having between about 10 percent and about 75 percent by weight water. The fiber source can even be sheared while partially or fully submerged under a liquid, such as water, ethanol, isopropanol.
  • The fiber source can also be sheared in under a gas (such as a stream or atmosphere of gas other than air), e.g., oxygen or nitrogen, or steam.
  • Other methods of making the fibrous materials include, e.g., stone grinding, mechanical ripping or tearing, pin grinding or air attrition milling.
  • If desired, the fibrous materials can be separated, e.g., continuously or in batches, into fractions according to their length, width, density, material type, or some combination of these attributes. For example, for forming composites, it is often desirable to have a relatively narrow distribution of fiber lengths.
  • For example, ferrous materials can be separated from any of the fibrous materials by passing a fibrous material that includes a ferrous material past a magnet, e.g., an electromagnet, and then passing the resulting fibrous material through a series of screens, each screen having different sized apertures.
  • The fibrous materials can also be separated, e.g., by using a high velocity gas, e.g., air. In such an approach, the fibrous materials are separated by drawing off different fractions, which can be characterized photonically, if desired. Such a separation apparatus is discussed in Lindsey et al, U.S. Patent No. 6,883,667 .
  • The fibrous materials can irradiated immediately following their preparation, or they can may be dried, e.g., at approximately 105 °C for 4-18 hours, so that the moisture content is, e.g., less than about 0.5% before use.
  • If desired, lignin can be removed from any of the fibrous materials that include lignin. Also, to aid in the breakdown of the materials that include the cellulose, the material can be treated prior to irradiation with heat, a chemical (e.g., mineral acid, base or a strong oxidizer such as sodium hypochlorite) and/or an enzyme.
  • In some embodiments, the average opening size of the first screen is less than 0.79 mm (1/32 inch, 0.03125 inch), e.g., less than 0.51 mm (1/50 inch, 0.02000 inch), less than 0.40 mm (1/64 inch, 0.015625 inch), less than 0.23 mm (0.009 inch), less than 0.20 mm (1/128 inch, 0.0078125 inch), less than 0.18 mm (0.007 inch), less than 0.13 mm (0.005 inch), or even less than less than 0.10 mm (1/256 inch, 0.00390625 inch). The screen is prepared by interweaving monofilaments having an appropriate diameter to give the desired opening size. For example, the monofilaments can be made of a metal, e.g., stainless steel. As the opening sizes get smaller, structural demands on the monofilaments may become greater. For example, for opening sizes less than 0.40 mm, it can be advantageous to make the screens from monofilaments made from a material other than stainless steel, e.g., titanium, titanium alloys, amorphous metals, nickel, tungsten, rhodium, rhenium, ceramics, or glass. In some embodiments, the screen is made from a plate, e.g. a metal plate, having apertures, e.g., cut into the plate using a laser. In some embodiments, the open area of the mesh is less than 52%, e.g., less than 41%, less than 36%, less than 31%, less than 30%.
  • In some embodiments, the second fibrous is sheared and passed through the first screen, or a different sized screen. In some embodiments, the second fibrous material is passed through a second screen having an average opening size equal to or less than that of first screen.
  • Referring to FIG 4, a third fibrous material 220 can be prepared from the second fibrous material 216 by shearing the second fibrous material 216 and passing the resulting material through a second screen 222 having an average opening size less than the first screen 214.
  • Generally, the fibers of the fibrous materials can have a relatively large average length-to-diameter ratio (e.g., greater than 20-to-1), even if they have been sheared more than once. In addition, the fibers of the fibrous materials described herein may have a relatively narrow length and/or length-to-diameter ratio distribution.
  • As used herein, average fiber widths (i.e., diameters) are those determined optically by randomly selecting approximately 5,000 fibers. Average fiber lengths are corrected length-weighted lengths. BET (Brunauer, Emmet and Teller) surface areas are multi-point surface areas, and porosities are those determined by mercury porosimetry.
  • The average length-to-diameter ratio of the second fibrous material 14 can be, e.g. greater than 8/1, e.g., greater than 10/1, greater than 15/1, greater than 20/1, greater than 25l1, or greater than 50/1. An average length of the second fibrous material 14 can be, e.g., between about 0.5 mm and 2.5 mm, e.g., between about 0.75 mm and 1.0 mm, and an average width (i.e., diameter) of the second fibrous material 14 can be, e.g., between about 5 µm and 50 µm, e.g., between about 10 µm and 30 µm.
  • In some embodiments, a standard deviation of the length of the second fibrous material 14 is less than 60 percent of an average length of the second fibrous material 14, e.g., less than 50 percent of the average length, less than 40 percent of the average length, less than 25 percent of the average length, less than 10 percent of the average length, less than 5 percent of the average length, or even less than 1 percent of the average length.
  • In some embodiments, a BET surface area of the second fibrous material is greater than 0.1 m2/g, e.g., greater than 0.25 m2/g, greater than 0.5 m2/g, greater than 1.0 m2/g, greater than 1.5 m2/g, greater than 1.75 m2/g, greater than 5.0 m2/g, greater than 10 m2/g, greater than 25 m2/g, greater than 35 m2/g, greater than 50m2/g, greater than 60 m2/g, greater than 75 m2/g, greater than 100 m2/g, greater than 150 m2/g, greater than 200 m2/g, or even greater than 250 m2/g. A porosity of the second fibrous material 14 can be, e.g., greater than 20 percent, greater than 25 percent, greater than 35 percent, greater than 50 percent, greater than 60 percent, greater than 70 percent, e.g., greater than 80 percent, greater than 85 percent, greater than 90 percent, greater than 92 percent, greater than 94 percent, greater than 95 percent, greater than 97.5 percent, greater than 99 percent, or even greater than 99.5 percent.
  • In some embodiments, a ratio of the average length-to-diameter ratio of the first fibrous material to the average length-to-diameter ratio of the second fibrous material is, e.g., less than 1.5, e.g., less than 1.4, less than 1.25, less than 1.1, less than 1.075, less than 1.05, less than 1.025, or even substantially equal to 1.
  • In particular embodiments, the second fibrous material is sheared again and the resulting fibrous material passed through a second screen having an average opening size less than the first screen to provide a third fibrous material. In such instances, a ratio of the average length-to-diameter ratio of the second fibrous material to the average length-to-diameter ratio of the third fibrous material can be, e.g., less than 1.5, e.g., less than 1.4, less than 1.25, or even less than 1.1.
  • In some embodiments, the third fibrous material is passed through a third screen to produce a fourth fibrous material. The fourth fibrous material can be, e.g., passed through a fourth screen to produce a fifth material. Similar screening processes can be repeated as many times as desired to produce the desired fibrous material having the desired properties.
  • Densification
  • Densified materials can be processed by any of the methods described herein.
  • A material, e.g., a fibrous material, having a low bulk density can be densified to a product having a higher bulk density. For example, a material composition having a bulk density of 0.05 g/ cm3 can be densified by sealing the fibrous material in a relatively gas impermeable structure, e.g., a bag made of polyethylene or a bag made of alternating layers of polyethylene and a nylon, and then evacuating the entrapped gas, e.g., air, from the structure. After evacuation of the air from the structure, the fibrous material can have, e.g., a bulk density of greater than 0.3 g/cm3, e.g., 0.5 g/cm3, 0.6 g/cm3, 0.7 g/cm3 or more, e.g., 0.85 g/ cm3. After densification, the product can processed by any of the methods described herein, e.g., irradiated, e.g., with gamma radiation. This can be advantageous when it is desirable to transport the material to another location, e.g., a remote manufacturing plant, where the fibrous material composition can be added to a solution, e.g., to produce ethanol. After piercing the substantially gas impermeable structure, the densified fibrous material can revert to nearly its initial bulk density, e.g., greater than 60 percent of its initial bulk density, e.g., 70 percent, 80 percent, 85 percent or more, e.g., 95 percent of its initial bulk density. To reduce static electricity in the fibrous material, an anti-static agent can be added to the material.
  • In some embodiments, the structure, e.g., bag, is formed of a material that dissolves in a liquid, such as water. For example, the structure can be formed from a polyvinyl alcohol so that it dissolves when in contact with a water-based system. Such embodiments allow densified structures to be added directly to solutions that include a microorganism, without first releasing the contents of the structure, e.g., by cutting.
  • Referring to FIG. 5, a biomass material can be combined with any desired additives and a binder, and subsequently densified by application of pressure, e.g., by passing the material through a nip defined between counter-rotating pressure rolls or by passing the material through a pellet mill. During the application of pressure, heat can optionally be applied to aid in the densification of the fibrous material The densified material can then be irradiated.
  • In some embodiments, the material prior to densification has a bulk density of less than 0.25 g/cm3, e.g., 0.20 g/cm3, 0.15 g/cm3, 0.10 g/cm3, 0.05 g/cm3 or less, e.g., 0.025 g/cm3. Bulk density is determined using ASTM D1895B. Briefly, the method involves filling a measuring cylinder of known volume with a sample and obtaining a weight of the sample. The bulk density is calculated by dividing the weight of the sample in grams by the known volume of the cylinder in cubic centimeters.
  • The preferred binders include binders that are soluble in water, swollen by water, or that has a glass transition temperature of less 25 °C, as determined by differential scanning calorimetry. By water-soluble binders, we mean binders having a solubility of at least about 0.05 weight percent in water. By water swellable binders, we mean binders that increase in volume by more than 0.5 percent upon exposure to water.
  • In some embodiments, the binders that are soluble or swollen by water include a functional group that is capable of forming a bond, e.g., a hydrogen bond, with the fibers of the fibrous material, e.g., cellulosic fibrous material. For example, the functional group can be a carboxylic acid group, a carboxylate group, a carbonyl group, e.g., of an aldehyde or a ketone, a sulfonic acid group, a sulfonate group, a phosphoric acid group, a phosphate group, an amide group, an amine group, a hydroxyl group, e.g., of an alcohol, and combinations of these groups, e.g., a carboxylic acid group and a hydroxyl group. Specific monomeric examples include glycerin, glyoxal, ascorbic acid, urea, glycine, pentaerythritol, a monosaccharide or a disaccharide, citric acid, and tartaric acid. Suitable saccharides include glucose, sucrose, lactose, ribose, fructose, mannose, arabinose and ecythrose. Polymeric examples include polyglycols, polyethylene oxide, polycarboxylic acids, polyamides, polyamines and polysulfonic acids polysulfonates. Specific polymeric examples include polypropylene glycol (PPG), polyethylene glycol (PEG), polyethylene oxide, e.g., POLYOX®, copolymers of ethylene oxide and propylene oxide, polyacrylic acid (PAA), polyacrylamide, polypeptides, polyethylenimine, polyvinylpyridine, poly(sodium-4-styrenesulfonate) and poly(2-acrylamidomethyl-1-propanesulfonic acid).
  • In some embodiments, the binder includes a polymer that has a glass transition temperature less 25 °C. Examples of such polymers include thermoplastic elastomers (TPEs). Examples ofTPEs include polyether block amides, such as those available under the tradename PEBAX®, polyester elastomers, such as those available under the tradename HYTREL®, and styrenic block copolymers, such as those available under the tradename KRATON®. Other suitable polymers having a glass transition temperature less 25 °C include ethylene vinyl acetate copolymer (EVA), polyolefins, e.g., polyethylene, polypropylene, ethylene-propylene copolymers, and copolymers of ethylene and alpha olefins, e.g., 1-octene, such as those available under the tradename ENGAGE®. In some embodiments, e.g., when the material is a fiberized polycoated paper, the material is densified without the addition of a separate low glass transition temperature polymer.
  • In a particular embodiment, the binder is a lignin, e.g., a natural or synthetically modified lignin.
  • A suitable amount of binder added to the material, calculated on a dry weight basis, is, e.g., from about 0.01 percent to about 50 percent, e.g., 0.03 percent, 0.05 percent, 0.1 percent, 0.25 percent, 0.5 percent, 1.0 percent, 5 percent, 10 percent or more, e.g., 25 percent, based on a total weight of the densified material. The binder can be added to the material as a neat, pure liquid, as a liquid having the binder dissolved therein, as a dry powder of the binder, or as pellets of the binder.
  • The densified fibrous material can be made in a pellet mill. Referring to FIG 6, a pellet mill 300 has a hopper 301 for holding undensified material 310 that includes a carbohydrate-containing materials, such as cellulose. The hopper communicates with an auger 312 that is driven by variable speed motor 314 so that undensified material can be transported to a conditioner 320 that stirs the undensified material with paddles 322 that are rotated by conditioner motor 330. Other ingredients, e.g., any of the additives and/or fillers described herein, can be added at inlet 332. If desired, heat may be added while the fibrous material is in conditioner. After conditioned, the material passes from the conditioner through a dump chute 340, and to another auger 342. The dump chute, as controlled by actuator 344, allows for unobstructed passage of the material from conditioner to auger. Auger is rotated by motor 346, and controls the feeding of the fibrous material into die and roller assembly 350. Specifically, the material is introduced into a hollow, cylindrical die 352, which rotates about a horizontal axis and which has radially extending die holes 250. Die 352 is rotated about the axis by motor 360, which includes a horsepower gauge, indicating total power consumed by the motor. Densified material 370, e.g., in the form of pellets, drops from chute 372 and are captured and processed, such as by irradiation.
  • The material, after densification, can be conveniently in the form of pellets or chips having a variety of shapes. The pellets can then be irradiated. In some embodiments, the pellets or chips are cylindrical in shape, e.g., having a maximum transverse dimension of, e.g., 1 mm or more, e.g., 2 mm, 3 mm, 5 mm, 8 mm, 10 mm, 15 mm or more, e.g., 25 mm. Another convenient shape for making composites includes pellets or chips that are plate-like in form, e.g., having a thickness of 1 mm or more, e.g., 2 mm, 3 mm, 5 mm, 8 mm, 10 mm or more, e.g., 25 mm; a width of, e.g., 5 mm or more, e.g., 10 mm, 15 mm, 25 mm, 30 mm or more, e.g., 50 mm; and a length of 5 mm or more, e.g., 10 mm, 15 mm, 25 mm, 30 mm or more, e.g., 50 mm.
  • Referring now FIG 7A-7D, pellets can be made so that they have a hollow inside. As shown, the hollow can be generally in-line with the center of the pellet (FIG. 7B), or out of line with the center of the pellet (FIG 7C). Making the pellet hollow inside can increase the rate of dissolution in a liquid after irradiation.
  • Referring now to FIG 7D, the pellet can have, e.g., a transverse shape that is multilobal, e.g., tri-lobal as shown, or tetra-lobal, penta-lobal, hexa-lobal or deca-lobal. Making the pellets in such transverse shapes can also increase the rate of dissolution in a solution after irradiation.
  • Examples
  • In one example, half-gallon juice cartons made of un-printed white Kraft board having a bulk density of 20 lb/ft3 can be used as a feedstock. Cartons can be folded flat and then fed into a shredder to produce a confetti-like material having a width of between 0.1 inch and 0.5 inch, a length of between 0.25 inch and 1 inch and a thickness equivalent to that of the starting material (about 0.075 inch). The confetti-like material can be fed to a rotary knife cutter which shears the confetti-like pieces, tearing the pieces apart and releasing fibrous material.
  • In some cases, multiple shredder-shearer trains can be arranged in series with output. In one embodiment, two shredder-shearer trains can be arranged in series with output from the first shearer fed as input to the second shredder. In another embodiment, three shredder-shearer trains can be arranged in series with output from the first shearer fed as input to the second shredder and output from the second shearer fed as input to the third shredder. Multiple passes through shredder-shearer trains are anticipated to increase decrease particle size and increase overall surface area within the feedstream.
  • In another example, fibrous material produced from shredding and shearing juice cartons can be treated to increase its bulk density. In some cases, the fibrous material can be sprayed with water or a dilute stock solution of POLYOX WSR N10 (polyethylene oxide) prepared in water. The wetted fibrous material can then be processed through a pellet mill operating at room temperature. The pellet mill can increase the bulk density of the feedstream by more than an order of magnitude.
  • PRETREATMENT
  • Physically prepared feedstock can be pretreated for use in primary production processes by, for example, reducing the average molecular weight and crystallinity of the feedstock and/or increasing the surface area and/or porosity of the feedstock Pretreatment processes can include one or more of irradiation, sonication, oxidation, pyrolysis, and steam explosion. The various pretreatment systems and methods can be used in combinations of two, three, or even four of these technologies.
  • Pretreatment Combinations
  • In some embodiments, biomass can be processed by applying two or more of any of the processes described herein, such as two or more of radiation, sonication, oxidation, pyrolysis, and steam explosion either with or without prior, intermediate, or subsequent feedstock preparation as described herein. The processes can be applied in any order (or concurrently) to the biomass, e.g., a cellulosic and/or lignocellulosic material. In other embodiments, materials that include a carbohydrate are prepared by applying three, four or more of any of the processes described herein (in any order or concurrently). For example, a carbohydrate can be prepared by applying radiation, sonication, oxidation, pyrolysis, and, optionally, steam explosion to a cellulosic and/or lignocellulosic material (in any order or concurrently). The provided carbohydrate-containing material can then be converted by one or more microorganisms, such as bacteria, yeast, or mixtures of yeast and bacteria, to a number of desirable products, as described herein. Multiple processes can provide materials that can be more readily utilized by a variety of microorganisms because of their lower molecular weight, lower crystallinity, and/or enhanced solubility. Multiple processes can provide synergies and can reduce overall energy input required in comparison to any single process.
  • For example, in some embodiments, feedstocks are provided that include a carbohydrate that is produced by a process that includes irradiating and sonicating (in either order or concurrently) a cellulosic and/or a lignocellulosic material, a process that includes irradiating and oxidizing (in either order or concurrently) a cellulosic and/or a lignocellulosic material, a process that includes irradiating and pyrolyzing (in either order or concurrently) a cellulosic and/or a lignocellulosic material, a process that includes irradiating and pyrolyzing (in either order or concurrently) a cellulosic and/or a lignocellulosic material, or a process that includes irradiating and steam-exploding (in either order or concurrently) a cellulosic and/or a lignocellulosic material. The provided feedstock can then be contacted with a microorganism having the ability to convert at least a portion, e.g., at least about 1 percent by weight, of the feedstock to the product, such as the combustible fuel, as described herein.
  • In some embodiments, the process does not include hydrolyzing the cellulosic and/or lignocellulosic material, such as with an acid or a base, e.g., a mineral acid, such as hydrochloric or sulfuric acid.
  • If desired, some or none of the feedstock can include a hydrolyzed material. For example, in some embodiments, at least about seventy percent by weight of the feedstock is an unhydrolyzed material, e.g., at least at 95 percent by weight of the feedstock is an unhydrolyzed material. In some embodiments, substantially all of the feedstock is an unhydrolyzed material.
  • Any feedstock or any reactor or fermentor charged with a feedstock can include a buffer, such as sodium bicarbonate, ammonium chloride or Tris; an electrolyte, such as potassium chloride, sodium chloride, or calcium chloride; a growth factor, such as biotin and/or a base pair such as uracil or an equivalent thereof; a surfactant, such as Tween® or polyethylene glycol; a mineral, such as such as calcium, chromium, copper, iodine, iron, selenium, or zinc; or a chelating agent, such as ethylene diamine, ethylene diamine tetraacetic acid (EDTA) (or its salt form, e.g., sodium or potassium EDTA), or dimercaprol.
  • When radiation is utilized, it can be applied to any sample that is dry or wet, or even dispersed in a liquid, such as water. For example, irradiation can be performed on cellulosic and/or lignocellulosic material in which less than about 25 percent by weight of the cellulosic and/or lignocellulosic material has surfaces wetted with a liquid, such as water. In some embodiments, irradiating is performed on cellulosic and/or lignocellulosic material in which substantially none of the cellulosic and/or lignocellulosic material is wetted with a liquid, such as water.
  • In some embodiments, any processing described herein occurs after the cellulosic and/or lignocellulosic material remains dry as acquired or has been dried, e.g., using heat and/or reduced pressure. For example, in, some embodiments, the cellulosic and/or lignocellulosic material has less than about five percent by weight retained water, measured at 25°C and at fifty percent relative humidity.
  • If desired, a swelling agent, as defined herein, can be utilized in any process described herein. In some embodiments, when a cellulosic and/or lignocellulosic material is processed using radiation, less than about 25 percent by weight of the cellulosic and/or lignocellulosic material is in a swollen state, the swollen state being characterized as having a volume of more than about 2.5 percent higher than an unswollen state, e.g., more than 5.0, 7.5, 10, or 15 percent higher than the unswollen state. In some embodiments, when radiation is utilized on a cellulosic and/or lignocellulosic material, substantially none of the cellulosic and/or lignocellulosic material is in a swollen state.
  • In specific embodiments when radiation is utilized, the cellulosic and/or lignocellulosic material includes a swelling agent, and swollen cellulosic and/or lignocellulosic receives a dose of less than about 10 Mrad.
  • When radiation is utilized in any process, it can be applied while the cellulosic and/or lignocellulosic is exposed to air, oxygen-enriched air, or even oxygen itself, or blanketed by an inert gas such as nitrogen, argon, or helium. When maximum oxidation is desired, an oxidizing environment is utilized, such as air or oxygen.
  • When radiation is utilized, it may be applied to biomass, such as cellulosic and/or lignocellulosic material, under a pressure of greater than about 2.5 atmospheres, such as greater than 5, 10, 15, 20 or even greater than about 50 atmospheres.
  • In specific embodiments, the process includes irradiating and sonicating and irradiating precedes sonicating. In other specific embodiments, sonication precedes irradiating, or irradiating and sonicating occur concurrently.
  • In some embodiments, the process includes irradiating and sonicating (in either order or concurrently) and further includes oxidizing, pyrolyzing or steam exploding.
  • When the process includes radiation, the irradiating can be performed utilizing an ionizing radiation, such as gamma rays, x-rays, energetic ultraviolet radiation, such as ultraviolet C radiation having a wavelength of from about 100 nm to about 280 nm, a beam of particles, such as a beam of electrons, slow neutrons or alpha particles. In some embodiments, irradiating includes two or more radiation sources, such as gamma rays and a beam of electrons, which can be applied in either order or concurrently.
  • In specific embodiments, sonicating can performed at a frequency of between about 15khz and about 25khz, such as between about 18khz and 22khz utilizing a 1 KW or larger horn, e.g., a 2, 3, 4, 5, or even a 10 KW horn.
  • In some embodiments, the cellulosic and/or lignocellulosic material includes a first cellulose having a first number average molecular weight and the resulting carbohydrate includes a second cellulose having a second number average molecular weight lower than the first number average molecular weight. For example, the second number average molecular weight is lower than the first number average molecular weight by more than about twenty-five percent, e.g., 2x, 3x, 5x, 7x, 10x 25x, even 100x reduction.
  • In some embodiments, the first cellulose has a first crystallinity and the second cellulose has a second crystallinity lower than the first crystallinity, such as lower than about two, three, five, ten, fifteen or twenty-five percent lower.
  • In some embodiments, the first cellulose has a first level of oxidation and the second cellulose has a second level of oxidation higher than the first level of oxidation, such as two, three, four, five, ten or even twenty-five percent higher.
  • In one example of the use of radiation with oxidation as a pretreatment, half-gallon juice cartons made of un-printed polycoated white Kraft board having a bulk density of 20 lb/ft3 are used as a feedstock. Cartons are folded flat and then fed into a sequence of three shredder-shearer trains arranged in series with output from the first shearer fed as input to the second shredder, and output from the second shearer fed as input to the third shredder. The fibrous material produced by the can be sprayed with water and processed through a pellet mill operating at room temperature. The densified pellets can be placed in a glass ampoule which is sealed under an atmosphere of air. The pellets in the ampoule are irradiated with gamma radiation for about 3 hours at a dose rate of about 1 Mrad per hour to provide an irradiated material in which the cellulose has a lower molecular weight than the fibrous Kraft starting material.
  • Radiation Treatment
  • One or more irradiation processing sequences can be used to process raw feedstock from a wide variety of different sources to extract useful substances from the feedstock, and to provide partially degraded organic material which functions as input to further processing steps and/or sequences. Irradiation can reduce the molecular weight and/or crystallinity of feedstock. In some embodiments, energy deposited in a material that releases an electron from its atomic orbital is used to irradiate the materials. The radiation may be provided by 1) heavy charged particles, such as alpha particles, 2) electrons, produced, for example, in beta decay or electron beam accelerators, or 3) electromagnetic radiation, for example, gamma rays, x rays, or ultraviolet rays. In one approach, radiation produced by radioactive substances can be used to irradiate the feedstock. In another approach, electromagnetic radiation (e.g., produced using electron beam emitters) can be used to irradiate the feedstock. The doses applied depend on the desired effect and the particular feedstock. For example, high doses of radiation can break chemical bonds within feedstock components and low doses of radiation can increase chemical bonding (e.g., cross-linking) within feedstock components.
  • Referring to FIG. 8, in one method, a first material 2 that is or includes cellulose having a first number average molecular weight (TMN1) is irradiated, e.g., by treatment with ionizing radiation (e.g., in the form of gamma radiation, X-ray radiation, 100 mn to 280 nm ultraviolet (UV) light, a beam of electrons or other charged particles) to provide a second material 3 that includes cellulose having a second number average molecular weight (TMN2) lower than the first number average molecular weight. The second material (or the first and second material) can be combined with a microorganism (e.g., a bacterium or a yeast) that can utilize the second and/or first material to produce a fuel 5 that is or includes hydrogen, an alcohol (e.g., ethanol or butanol, such as n-, sec- or t-butanol), an organic acid, a hydrocarbon or mixtures of any of these.
  • Since the second material 3 has cellulose having a reduced molecular weight relative to the first material, and in some instances, a reduced crystallinity as well, the second material is generally more dispersible, swellable and/or soluble in a solution containing a microorganism. These properties make the second material 3 more susceptible to chemical, enzymatic and/or biological attack relative to the first material 2, which can greatly improve the production rate and/or production level of a desired product, e.g., ethanol. Radiation can also sterilize the materials.
  • In some embodiments, the second number average molecular weight (MN2) is lower than the first number average molecular weight (TMN1) by more than about 10 percent, e.g., 15, 20, 25, 30, 35, 40, 50 percent, 60 percent, or even more than about 75 percent
  • In some instances, the second material has cellulose that has as crystallinity (TC2) that is lower than the crystallinity (TC1) of the cellulose of the first material. For example, (TC2) can be lower than (TC1) by more than about 10 percent, e.g., 15, 20, 25, 30, 35, 40, or even more than about 50 percent.
  • In some embodiments, the starting crystallinity index (prior to irradiation) is from about 40 to about 87.5 percent, e.g., from about 50 to about 75 percent or from about 60 to about 70 percent, and the crystallinity index after irradiation is from about 10 to about 50 percent, e.g., from about 15 to about 45 percent or from about 20 to about 40 percent. However, in some embodiments, e.g., after extensive irradiation, it is possible to have a crystallinity index of lower than 5 percent. In some embodiments, the material after irradiation is substantially amorphous.
  • In some embodiments, the starting number average molecular weight (prior to irradiation) is from about 200,000 to about 3,200,000, e.g., from about 250,000 to about 1,000,000 or from about 250,000 to about 700,000, and the number average molecular weight after irradiation is from about 50,000 to about 200,000, e.g., from about 60,000 to about 150,000 or from about 70,000 to about 125,000. However, in some embodiments, e.g., after extensive irradiation, it is possible to have a number average molecular weight of less than about 10,000 or even less than about 5,000.
  • In some embodiments, the second material can have a level of oxidation (TO2) that is higher than the level of oxidation (TO1) of the first material. A higher level of oxidation of the material can aid in its dispersability, swellability and/or solubility, further enhancing the materials susceptibility to chemical, enzymatic or biological attack. In some embodiments, to increase the level of the oxidation of the second material relative to the first material, the irradiation is performed under an oxidizing environment, e.g., under a blanket of air or oxygen, producing a second material that is more oxidized than the first material. For example, the second material can have more hydroxyl groups, aldehyde groups, ketone groups, ester groups or carboxylic acid groups, which can increase its hydrophilicity.
  • Ionizing Radiation
  • Each form of radiation ionizes the biomass via particular interactions, as determined by the energy of the radiation. Heavy charged particles primarily ionize matter via Coulomb scattering; furthermore, these interactions produce energetic electrons that may further ionize matter. Alpha particles are identical to the nucleus of a helium atom and are produced by the alpha decay of various radioactive nuclei, such as isotopes of bismuth, polonium, astatine, radon, francium, radium, several actinides, such as actinium, thorium, uranium, neptunium, curium, californium, americium, and plutonium.
  • Electrons interact via Coulomb scattering and bremssthrahlung radiation produced by changes in the velocity of electrons. Electrons may be produced by radioactive nuclei that undergo beta decay, such as isotopes of iodine, cesium, technetium, and iridium. Alternatively, an electron gun can be used as an electron source via thermionic emission.
  • Electromagnetic radiation interacts via three processes: photoelectric absorption, Compton scattering, and pair production. The dominating interaction is determined by the energy of the incident radiation and the atomic number of the material. The summation of interactions contributing to the absorbed radiation in cellulosic material can be expressed by the mass absorption coefficient, graphed below as a function of incident energy.
    Figure imgb0003
  • Electromagnetic radiation is subclassified as gamma rays, x rays, ultraviolet rays, infrared rays, microwaves, or radiowaves, depending on its wavelength.
  • For example, gamma radiation can be employed to irradiate the materials. Referring to FIGS. 9 and 10 (an enlarged view of region R), a gamma irradiator 10 includes gamma radiation sources 408, e.g., 60Co pellets, a working table 14 for holding the materials to be irradiated and storage 16, e.g., made of a plurality iron plates, all of which are housed in a concrete containment chamber 20 that includes a maze entranceway 22 beyond a lead-lined door 26. Storage 16 includes a plurality of channels 30, e.g., sixteen or more channels, allowing the gamma radiation sources to pass through storage on their way proximate the working table.
  • In operation, the sample to be irradiated is placed on a working table. The irradiator is configured to deliver the desired dose rate and monitoring equipment is connected to an experimental block 31. The operator then leaves the containment chamber, passing through the maze entranceway and through the lead-lined door. The operator mans a control panel 32, instructing a computer 33 to lift the radiation sources 12 into working position using cylinder 36 attached to a hydraulic pump 40.
  • Gamma radiation has the advantage of a significant penetration depth into a variety of material in the sample. Sources of gamma rays include radioactive nuclei, such as isotopes of cobalt, calcium, technicium, chromium, gallium, indium, iodine, iron, krypton, samarium, selenium, sodium, thalium, and xenon.
  • Sources of x rays include electron beam collision with metal targets, such as tungsten or molybdenum or alloys, or compact light sources, such as those produced commercially by Lyncean.
  • Sources for ultraviolet radiation include deuterium or cadmium lamps.
  • Sources for infrared radiation include sapphire, zinc, or selenide window ceramic lamps.
  • Sources for microwaves include klystrons, Slevin type RF sources, or atom beam sources that employ hydrogen, oxygen, or nitrogen gases.
  • Electron Beam
  • In some embodiments, a beam of electrons is used as the radiation source. A beam of electrons has the advantages of high dose rates (e.g., 1, 5, or even 10 Mrad per second), high throughput, less containment, and less confinement equipment. Electrons can also be more efficient at causing chain scission. In addition, electrons having energies of 4-10 MeV can have a penetration depth of 5 to 30 mm or more, such as 40 mm.
  • Electron beams can be generated, e.g., by electrostatic generators, cascade generators, transformer generators, low energy accelerators with a scanning system, low energy accelerators with a linear cathode, linear accelerators, and pulsed accelerators. Electrons as an ionizing radiation source can be useful, e.g., for relatively thin piles of materials, e.g., less than 0.5 inch, e.g., less than 0.4 inch, 0.3 inch, 0.2 inch, or less than 0.1 inch. In some embodiments, the energy of each electron of the electron beam is from about 0.3 MeV to about 2.0 MeV (million electron volts), e.g., from about 0.5 MeV to about 1.5 MeV, or from about 0.7 MeV to about 1.25 MeV.
  • FIG. 11 shows a process flow diagram 3000 that includes various steps in an electron beam irradiation feedstock pretreatment sequence. In first step 3010, a supply of dry feedstock is received from a feed source. As discussed above, the dry feedstock from the feed source may be pre-processed prior to delivery to the electron beam irradiation devices. For example, if the feedstock is derived from plant sources, certain portions of the plant material may be removed prior to collection of the plant material and/or before the plant material is delivered by the feedstock transport device. Alternatively, or in addition, as expressed in optional step 3020, the biomass feedstock can be subjected to mechanical processing (e.g., to reduce the average length of fibers in the feedstock) prior to delivery to the electron beam irradiation devices.
  • In step 3030, the dry feedstock is transferred to a feedstock transport device (e.g., a conveyor belt) and is distributed over the cross-sectional width of the feedstock transport device approximately uniformly by volume. This can be accomplished, for example, manually or by inducing a localized vibration motion at some point in the feedstock transport device prior to the electron beam irradiation processing.
  • In some embodiments, a mixing system introduces a chemical agent 3045 into the feedstock in an optional process 3040 that produces a slurry. Combining water with the processed feedstock in mixing step 3040 creates an aqueous feedstock slurry that may be transported through, for example, piping rather than using, for example, a conveyor belt.
  • The next step 3050 is a loop that encompasses exposing the feedstock (in dry or slurry form) to electron beam radiation via one or more (say, N) electron beam irradiation devices. The feedstock slurry is moved through each of the N "showers" of electron beams at step 3052. The movement may either be at a continuous speed through and between the showers, or there may be a pause through each shower, followed by a sudden movement to the next shower. A small slice of the feedstock slurry is exposed to each shower for some predetermined exposure time at step 3053.
  • Electron beam irradiation devices may be procured commercially from Ion Beam Applications, Louvain-la-Neuve, Belgium or the Titan Corporation, San Diego, CA. Typical electron energies can be 1 MeV, 2 MeV, 4.5 MeV, 7.5 MeV, or 10 MeV. Typical electron beam irradiation device power can be 1 kW, 5 kW, 10 kW, 20 kW, 50 kW, 100 kW, 250 kW, or 500 kW. Effectiveness of depolymerization of the feedstock slurry depends on the electron energy used and the dose applied, while exposure time depends on the power and dose. Typical doses may take values of 1 kGy, 5 kGy, 10 kGy, 20 kGy, 50 kGy, 100 kGy, or 200 kGy.
  • Tradeoffs in considering electron beam irradiation device power specifications include cost to operate, capital costs, depreciation, and device footprint. Tradeoffs in considering exposure dose levels of electron beam irradiation would be energy costs and environment, safety, and health (ESH) concerns. Tradeoffs in considering electron energies include energy costs; here, a lower electron energy may be advantageous in encouraging depolymerization of certain feedstock slurry (see, for example, Bouchard, et al, Cellulose (2006) 13: 601-610).
  • It may be advantageous to provide a double-pass of electron beam irradiation in order to provide a more effective depolymerization process. For example, the feedstock transport device could direct the feedstock (in dry or slurry form) underneath and in a reverse direction to its initial transport direction. Double-pass systems can allow thicker feedstock slurries to be processed and can provide a more uniform depolymerization through the thickness of the feedstock slurry.
  • The electron beam irradiation device can produce either a fixed beam or a scanning beam. A scanning beam may be advantageous with large scan sweep length and high scan speeds, as this would effectively replace a large, fixed beam width. Further, available sweep widths of 0.5 m, 1m, 2 m or more are available.
  • Once a portion of feedstock slurry has been transported through the N electron beam irradiation devices, it may be necessary in some embodiments, as in step 3060, to mechanically separate the liquid and solid components of the feedstock slurry. In these embodiments, a liquid portion of the feedstock slurry is filtered for residual solid particles and recycled back to the slurry preparation step 3040. A solid portion of the feedstock slurry is then advanced on to the next processing step 3070 via the feedstock transport device. In other embodiments, the feedstock is maintained in slurry form for further processing.
  • Electromagnetic Radiation
  • In embodiments in which the irradiating is performed with electromagnetic radiation, the electromagnetic radiation can have, e.g., energy per photon (in electron volts) of greater than 102 eV, e.g., greater than 103, 104, 105, 106, or even greater than 167 eV. In some embodiments, the electromagnetic radiation has energy per photon of between 104 and 107, e.g., between 105 and 106 eV. The electromagnetic radiation can have a frequency of, e.g., greater than 1016 hz, greater than 1017 hz, 1018, 1019, 1020, or even greater than 1021 hz. In some embodiments, the electromagnetic radiation has a frequency of between 1018 and 1022 hz, e.g., between 1019 to 1021 hz.
  • Doses
  • In some embodiments, the irradiating (with any radiation source or a combination of sources) is performed until the material receives a dose of at least 0.25 Mrad, e.g., at least 1.0 Mrad, at least 2.5 Mrad, at least 5.0 Mrad, or at least 10.0 Mrad. In some embodiments, the irradiating is performed until the material receives a dose of between 1.0 Mrad and 6.0 Mrad, e.g., between 1.5 Mrad and 4.0 Mrad.
  • In some embodiments, the irradiating is performed at a dose rate of between 5.0 and 1500.0 kilorads/hour, e.g., between 10.0 and 750.0 kilorads/hour or between 50.0 and 350.0 kilorads/hours.
  • In some embodiments, two or more radiation sources are used, such as two or more ionizing radiations. For example, samples can be treated, in any order, with a beam of electrons, followed by gamma radiation and UV light having wavelengths from about 100 nm to about 280 nm. In some embodiments, samples are treated with three ionizing radiation sources, such as a beam of electrons, gamma radiation, and energetic UV light.
  • In some embodiments, relatively low doses of radiation can crosslink, graft, or otherwise increase the molecular weight of a carbohydrate-containing material, such as a cellulosic or lignocellulosic material (e.g., cellulose). Such a material having increased molecular weight can be useful, e.g., in making a composite, e.g., having improved mechanical properties, such as abrasion resistance, compression strength, fracture resistance, impact strength, bending strength, tensile modulus, flexural modulus and elongation at break. Such a material having increased molecular weight can be useful in making a composition.
  • For example, a fibrous material that includes a first cellulosic and/or lignocellulosic material having a first molecular weight can be irradiated in such a manner as to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight. For example, if gamma radiation is utilized as the radiation source, a dose of from about 1 Mrad to about 10 Mrad, e.g., from about 1.5 Mrad to about 7.5 Mrad or from about 2.0 Mrad to about 5.0 Mrad, can be applied. After the low dose of radiation, the second cellulosic and/or lignocellulosic material can be combined with a resin and formed into a composite, e.g., by compression molding, injection molding; or extrusion. Forming composites is described in WO 2006/102543 , and in U.S. Provisional Patent Application Serial Nos. 60/664,832, filed on March 24, 2005 , 60/688,002, filed on June 7, 2005 , 601711,057, filed on August 24, 2005 , 60/715,822, filed on September 9, 2005 , 60/725,674, filed on October 12, 2005 , 60/726,102, filed on October 12,2005 , and 60/750,205, filed on December 13,2005 .
  • Alternatively, a fibrous material that includes a first cellulosic and/or lignocellulosic material having a first molecular weight can be combined with a resin to provide a composite, and then the composite can be irradiated with a relatively low dose of radiation so as to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight. For example, if gamma radiation is utilized as the radiation source, a dose of from about 1 Mrad to about 10 Mrad can be applied. Using this approach increases the molecular weight of the material while it is with a resin matrix. In some embodiments, the resin is a cross-linkable resin and as such it crosslinks as the carbohydrate-containing material increases in molecular weight, which can provide a synergistic effect to provide maximum mechanical properties to the composite. For example, such composites can have excellent low temperature performance, e.g., having a reduced tendency to break and/or crack at low temperatures, e.g., temperatures below 0 °C, e.g., below -10 °C, -20 °C, -40 °C, -50 °C, -60 °C or even below -100 °C, and/or excellent performance at high temperatures, e.g., capable of maintaining their advantageous mechanical properties at relatively high temperature, e.g., at temperatures above 100 °C, e.g., above 125 °C, 150 °C, 200 °C, 250 °C, 300 °C, 400 °C, or even above 500 °C. In addition, such composites can have excellent chemical resistance, e.g., resistance to swelling in a solvent, e.g., a hydrocarbon solvent, resistance to chemical attack, e.g., by strong acids, strong bases, strong oxidants (e.g., chlorine or bleach) or reducing agents (e.g., active metals such as sodium and potassium).
  • Alternatively, in another example, a fibrous material that includes a cellulosic and/or lignocellulosic material is irradiated and, optionally, treated with acoustic energy, e.g., ultrasound.
  • In one example of the use of radiation as a pretreatment, half-gallon juice cartons made of un-printed polycoated white Kraft board having a bulk density of 20 lb/ft3 are used as a feedstock. Cartons are folded flat and then fed into a sequence of three shredder-shearer trains arranged in series with output from the first shearer fed as input to the second shredder, and output from the second shearer fed as input to the third shredder. The fibrous material produced by the can be sprayed with water and processed through a pellet mill operating at room temperature. The densified pellets can be placed in a glass ampoule which is evacuated under high vacuum and then back-filled with argon gas. The ampoule is sealed under argon. The pellets in the ampoule are irradiated with gamma radiation for about 3 hours at a dose rate of about 1 Mrad per hour to provide an irradiated material in which the cellulose has a lower molecular weight than the starting material.
  • Sonication
  • One or more sonication processing sequences can be used to process raw feedstock from a wide variety of different sources to extract useful substances from the feedstock, and to provide partially degraded organic material which functions as input to further processing steps and/or sequences. Sonication can reduce the molecular weight and/or crystallinity of feedstock.
  • Referring again to FIG. 8, in one method, a first material 2 that includes cellulose having a first number average molecular weight (TMN1) is dispersed in a medium, such as water, and sonicated and/or otherwise cavitated, to provide a second material 3 that includes cellulose having a second number average molecular weight (TMN2) lower than the first number average molecular weight. The second material (or the first and second material in certain embodiments) can be combined with a microorganism (e.g., a bacterium or a yeast) that can utilize the second and/or first material to produce a fuel 5 that is or includes hydrogen, an alcohol, an organic acid, a hydrocarbon or mixtures of any of these.
  • Since the second material has cellulose having a reduced molecular weight relative to the first material, and in some instances, a reduced crystallinity as well, the second material is generally more dispersible, swellable, and/or soluble in a solution containing the microorganism, e.g., at a concentration of greater than 106 microorganisms/mL. These properties make the second material 3 more susceptible to chemical, enzymatic, and/or microbial attack relative to the first material 2, which can greatly improve the production rate and/or production level of a desired product, e.g., ethanol. Sonication can also sterilize the materials, but should not be used while the microorganisms are supposed to be alive.
  • In some embodiments, the second number average molecular weight (TMN2) is lower than the first number average molecular weight (TMN1) by more than about 10 percent, e.g., 15, 20, 25, 30, 35, 40, 50 percent, 60 percent, or even more than about 75 percent.
  • In some instances, the second material has cellulose that has as crystallinity (TC2) that is lower than the crystallinity (TC1) of the cellulose of the first material. For example, (TC2) can be lower than (TC1) by more than about 10 percent, e.g.,15, 20, 25, 30, 35, 40, or even more than about 50 percent.
  • In some embodiments, the starting crystallinity index (prior to sonication) is from about 40 to about 87.5 percent, e.g., from about 50 to about 75 percent or from about 60 to about 70 percent, and the crystallinity index after sonication is from about 10 to about 50 percent, e.g., from about 15 to about 45 percent or from about 20 to about 40 percent However, in certain embodiments, e.g., after extensive sonication, it is possible to have a crystallinity index of lower than 5 percent. In some embodiments, the material after sonication is substantially amorphous.
  • In some embodiments, the starting number average molecular weight (prior to sonication) is from about 200,000 to about 3,200,000, e.g., from about 250,000 to about 1,000,000 or from about 250,000 to about 700,000, and the number average molecular weight after sonication is from about 50,000 to about 200,000, e.g., from about 60,000 to about 150,000 or from about 70,000 to about 125,000. However, in some embodiments, e.g., after extensive sonication, it is possible to have a number average molecular weight of less than about 10,000 or even less than about 5,000.
  • In some embodiments, the second material can have a level of oxidation (TO2) that is higher than the level of oxidation (TO1) of the first material. A higher level of oxidation of the material can aid in its dispersability, swellability and/or solubility, further enhancing the materials susceptibility to chemical, enzymatic or microbial attack. In some embodiments, to increase the level of the oxidation of the second material relative to the first material, the sonication is performed in an oxidizing medium, producing a second material that is more oxidized than the first material. For example, the second material can have more hydroxyl groups, aldehyde groups, ketone groups, ester groups or carboxylic acid groups, which can increase its hydrophilicity.
  • In some embodiments, the sonication medium is an aqueous medium. If desired, the medium can include an oxidant, such as a peroxide (e.g., hydrogen peroxide), a dispersing agent and/or a buffer. Examples of dispersing agents include ionic dispersing agents, e.g., sodium lauryl sulfate, and non-ionic dispersing agents, e.g., poly(ethylene glycol).
  • In other embodiments, the sonication medium is non-aqueous. For example, the sonication can be performed in a hydrocarbon, e.g., toluene or heptane, an ether, e.g., diethyl ether or tetrahydrofuran, or even in a liquefied gas such as argon, xenon, or nitrogen.
  • Without wishing to be bound by any particular theory, it is believed that sonication breaks bonds in the cellulose by creating bubbles in the medium containing the cellulose, which grow and then violently collapse. During the collapse of the bubble, which can take place in less than a nanosecond, the implosive force raises the local temperature within the bubble to about 5100 K (even higher in some instance; see, e.g., Suslick et al., Nature 434,52-55) and generates pressures of from a few hundred atmospheres to over 1000 atmospheres or more. It is these high temperatures and pressures that break the bonds. In addition, without wishing to be bound by any particular theory, it is believed that reduced crystallinity arises, at least in part, from the extremely high cooling rates during collapse of the bubbles, which can be greater than about 1011 K/second. The high cooling rates generally do not allow the cellulose to organize and crystallize, resulting in materials that have reduced crystallinity. Ultrasonic systems and sonochemistry are discussed in, e.g., Olli et al., U.S. Patent No. 5,766,764 ; Roberts, U.S. Patent No. 5,828,156 ; Mason, Chemistry with Ultrasound, Elsevier, Oxford, (1990); Suslick (editor), Ultrasound: its Chemical, Physical and Biological Effects, VCH, Weinheim, (1988); Price, "Current Trends in Sonochemistry" Royal Society of Chemistry, Cambridge, (1992); Suslick et al., Ann. Rev. Mater. Sci. 29, 295, (1999); Suslick et al., Nature 353, 414 (1991); Hiller et al., Phys. Rev. Lett. 69,1182 (1992); Barber et al., Nature, 352, 414 (1991); Suslick et al., J. Am. Chem. Soc., 108, 5641 (1986); Tang et al., Chem. Comm., 2119 (2000); Wang et al., Advanced Mater., 12, 1137 (2000); Landau et al., J. of Catalysis, 201, 22 (2001); Perkas et al., Chem. Comm., 988 (2001); Nikitenko et al., Angew. Chem. Inter. Ed. (December 2001); Shafi et al., J. Phys. Chem B 103, 3358 (1999); Avivi et al., J. Amer. Chem. Soc. 121, 4196 (1999); and Avivi et al., J. Amer. Chem. Soc. 122, 4331 (2000).
  • Sonication Systems
  • FIG. 12 shows a general system in which a cellulosic material stream 1210 is mixed with a water stream 1212 in a reservoir 1214 to form a process stream 1216. A first pump 1218 draws process stream 1216 from reservoir 1214 and toward a flow cell 1224. Ultrasonic transducer 1226 transmits ultrasonic energy into process stream 1216 as the process stream flows through flow cell 1224. A second pump 1230 draws process stream 1216 from flow cell 1224 and toward subsequent processing.
  • Reservoir 1214 includes a first intake 1232 and a second intake 1234 in fluid communication with a volume 1236. A conveyor (not shown) delivers cellulosic material stream 1210 to reservoir 1214 through first intake 1232. Water stream 1212 enters reservoir 1214 through second intake 1234. In some embodiments, water stream 1212 enters volume 1236 along a tangent establishing a swirling flow within volume 1236. In certain embodiments, cellulosic material stream 1210 and water stream 1 FIG. 39 is a schematic view of a process for biomass conversion.
  • 212 are introduced into volume 1236 along opposing axes to enhance mixing within the volume.
  • Valve 1238 controls the flow of water stream 1212 through second intake 1232 to produce a desired ratio of cellulosic material to water (e.g., approximately 10% cellulosic material, weight by volume). For example, 2000 tons/day of cellulosic material can be combined with 1 million to 1.5 million gallons/day, e.g., 1.25 million gallons/day, of water.
  • Mixing of cellulosic material and water in reservoir 1214 is controlled by the size of volume 1236 and the flow rates of cellulosic material and water into the volume. In some embodiments, volume 1236 is sized to create a minimum mixing residence time for the cellulosic material and water. For example, when 2000 tons/day of cellulosic material and 1.25 million gallons/day of water are flowing through reservoir 1214, volume 1236 can be about 32,000 gallons to produce a minimum mixing residence time of about 15 minutes.
  • Reservoir 1214 includes a mixer 1240 in fluid communication with volume 1236. Mixer 1240 agitates the contents of volume 1236 to disperse cellulosic material throughout the water in the volume. For example, mixer 1240 can be a rotating vane disposed in reservoir 1214. In some embodiments, mixer 1240 disperses the cellulosic material substantially uniformly throughout the water.
  • Reservoir 1214 further includes an exit 1242 in fluid communication with volume 1236 and process stream 1216. The mixture of cellulosic material and water in volume 1236 flows out of reservoir 1214 via exit 1242. Exit 1242 is arranged near the bottom of reservoir 1214 to allow gravity to pull the mixture of cellulosic material and water out of reservoir 1214 and into process stream 1216.
  • First pump 1218 (e.g., any of several recessed impeller vortex pumps made by Essco Pumps & Controls, Los Angeles, California) moves the contents of process stream 1216 toward flow cell 1224. In some embodiments, first pump 1218 agitates the contents of process stream 1216 such that the mixture of cellulosic material and water is substantially uniform at inlet 1220 of flow cell 1224. For example, first pump 1218 agitates process stream 1216 to create a turbulent flow that persists along the process stream between the first pump and inlet 1220 of flow cell 1224.
  • Flow cell 1224 includes a reactor volume 1244 in fluid communication with inlet 1220 and outlet 1222. In some embodiments, reactor volume 1244 is a stainless steel tube capable of withstanding elevated pressures (e.g., 10 bars). In addition or in the alternative, reactor volume 1244 includes a rectangular cross section.
  • Flow cell 1224 further includes a heat exchanger 1246 in thermal communication with at least a portion of reactor volume 1244. Cooling fluid 1248 (e.g., water) flows into heat exchanger 1246 and absorbs heat generated when process stream 1216 is sonicated in reactor volume 1244. In some embodiments, the flow rate of cooling fluid 1248 into heat exchanger 1246 is controlled to maintain an approximately constant temperature in reactor volume 1244. In addition or in the alternative, the temperature of cooling fluid 1248 flowing into heat exchanger 1246 is controlled to maintain an approximately constant temperature in reactor volume 1244. In some embodiments, the temperature of reactor volume 1244 is maintained at 20 to 50°C, e.g., 25, 30, 35, 40, or 45°C. Additionally or alternatively, heat transferred to cooling fluid 1248 from reactor volume 1244 can be used in other parts of the overall process.
  • An adapter section 1226 creates fluid communication between reactor volume 1244 and a booster 1250 coupled (e.g., mechanically coupled using a flange) to ultrasonic transducer 1226. For example, adapter section 1226 can include a flange and O-ring assembly arranged to create a leak tight connection between reactor volume 1244 and booster 1250. In some embodiments, ultrasonic transducer 1226 is a high-powered ultrasonic transducer made by Hielscher Ultrasonics of Teltow, Germany.
  • In operation, a generator 1252 delivers electricity to ultrasonic transducer 1252. Ultrasonic transducer 1226 includes a piezoelectric element that converts the electrical energy into sound in the ultrasonic range. In some embodiments, the materials are sonicated using sound having a frequency of from about 16 kHz to about 110 kHz, e.g., from about 18 kHz to about 75 kHz or from about 20 kHz to about 40 kHz. (e.g., sound having a frequency of 20 kHz to 40 kHz).
  • The ultrasonic energy is then delivered to the working medium through booster 1248.
  • The ultrasonic energy traveling through booster 1248 in reactor volume 1244 creates a series of compressions and rarefactions in process stream 1216 with an intensity sufficient to create cavitation in process stream 1216. Cavitation disaggregates the cellulosic material dispersed in process stream 1216. Cavitation also produces free radicals in the water of process stream 1216. These free radicals act to further break down the cellulosic material in process stream 1216.
  • In general, 5 to 4000 MJ/m3, e.g., 10, 25, 50, 100, 250, 500, 750, 1000, 2000, or 3000 MJ/m3, of ultrasonic energy is applied to process stream 16 flowing at a rate of about 0.2 m3/s (about 3200 gallons/min). After exposure to ultrasonic energy in reactor volume 1244, process stream 1216 exits flow cell 1224 through outlet 1222. Second pump 1230 moves process stream 1216 to subsequent processing (e.g., any of several recessed impeller vortex pumps made by Essco Pumps & Controls, Los Angeles, California).
  • While certain embodiments have been described, other embodiments are possible.
  • As an example, while process stream 1216 has been described as a single flow path, other arrangements are possible. In some embodiments for example, process stream 1216 includes multiple parallel flow paths (e.g., flowing at a rate of 10 gallon/min). In addition or in the alternative, the multiple parallel flow paths of process stream 1216 flow into separate flow cells and are sonicated in parallel (e.g., using a plurality of 16 kW ultrasonic transducers).
  • As another example, while a single ultrasonic transducer 1226 has been described as being coupled to flow cell 1224, other arrangements are possible. In some embodiments, a plurality of ultrasonic transducers 1226 are arranged in flow cell 1224 (e.g., ten ultrasonic transducers can be arranged in a flow cell 1224). In some embodiments, the sound waves generated by each of the plurality of ultrasonic transducers 1226 are timed (e.g., synchronized out of phase with one another) to enhance the cavitation acting upon process stream 1216.
  • As another example, while a single flow cell 1224 has been described, other arrangements are possible. In some embodiments, second pump 1230 moves process stream to a second flow cell where a second booster and ultrasonic transducer further sonicate process stream 1216.
  • As still another example, while reactor volume 1244 has been described as a closed volume, reactor volume 1244 is open to ambient conditions in certain embodiments. In such embodiments, sonication pretreatment can be performed substantially simultaneously with other pretreatment techniques. For example, ultrasonic energy can be applied to process stream 1216 in reactor volume 1244 while electron beams are simultaneously introduced into process stream 1216.
  • As another example, while a flow through process has been described, other arrangements are possible. In some embodiments, sonication can be performed in a batch process. For example, a volume can be filled with a 10% (weight by volume) mixture of cellulosic material in water and exposed to sound with intensity from about 50 W/cm2 to about 600 W/cm2, e.g., from about 75 W/cm2 to about 300 W/cm2 or from about 95 W/cm2 to about 200 W/cm2. Additionally or alternatively, the mixture in the volume can be sonicated from about 1 hour to about 24 hours, e.g., from about 1.5 hours to about 12 hours, or from about 2 hours to about 10 hours. In certain embodiments, the material is sonicated for a pre-determined time, and then allowed to stand for a second pre-determined time before sonicating again.
  • Referring now to FIG. 13, in some embodiments, two electroacoustic transducers are mechanically coupled to a single horn. As shown, a pair of piezoelectric transducers 60 and 62 is coupled to a slotted bar horn 64 by respective intermediate coupling horns 70 and 72, the latter also being known as booster horns. The mechanical vibrations provided by the transducers, responsive to high frequency electrical energy applied thereto, are transmitted to the respective coupling horns, which may be constructed to provide a mechanical gain, such as a ratio of 1 to 1.2. The horns are provided with a respective mounting flange 74 and 76 for supporting the transducer and horn assembly in a stationary housing.
  • The vibrations transmitted from the transducers through the coupling or booster horns are coupled to the input surface 78 of the horn and are transmitted through the horn to the oppositely disposed output surface 80, which, during operation, is in forced engagement with a workpiece (not shown) to which the vibrations are applied.
  • The high frequency electrical energy provided by the power supply 82 is fed to each of the transducers, electrically connected in parallel, via a balancing transformer 84 and a respective series connected capacitor 86 and 90, one capacitor connected in series with the electrical connection to each of the transducers. The balancing transformer is known also as "balun" standing for "balancing unit." The balancing transformer includes a magnetic core 92 and a pair of identical windings 94 and 96, also termed the primary winding and secondary winding, respectively.
  • In some embodiments, the transducers include commercially available piezoelectric transducers, such as Branson Ultrasonics Corporation models 105 or 502, each designed for operation at 20 kHz and a maximum power rating of 3 kW. The energizing voltage for providing maximum motional excursion at the output surface of the transducer is 930 volt rms. The current flow through a transducer may vary between zero and 3.5 ampere depending on the load impedance. At 930 volt rms the output motion is approximately 20 microns. The maximum difference in terminal voltage for the same motional amplitude, therefore, can be 186 volt. Such a voltage difference can give rise to large circulating currents flowing between the transducers. The balancing unit 430 assures a balanced condition by providing equal current flow through the transducers, hence eliminating the possibility of circulating currents. The wire size of the windings must be selected for the full load current noted above and the maximum voltage appearing across a winding input is 93 volt.
  • As an alternative to using ultrasonic energy, high-frequency, rotor-stator devices can be utilized. This type of device produces high-shear, microcavitation forces which can disintegrate biomass in contact with such forces. Two commercially available high-frequency, rotor-stator dispersion devices are the Supraton devices manufactured by Krupp Industrietechnik GmbH and marketed by Dorr-Oliver Deutschland GmbH of Connecticut, and the Dispax devices manufactured and marketed by Ika-Works, Inc. of Cincinnati, Ohio. Operation of such a microcavitation device is discussed in Stuart, U.S. Patent No. 5,370,999 .
  • While ultrasonic transducer 1226 has been described as including one or more piezoelectric active elements to create ultrasonic energy, other arrangements are possible. In some embodiments, ultrasonic transducer 1226 includes active elements made of other types of magnetostrictive materials (e.g., ferrous metals). Design and operation of such a high-powered ultrasonic transducer is discussed in Hansen et al., U.S. Patent No. 6,624,539 . In some embodiments, ultrasonic energy is transferred to process stream 16 through an electrohydraulic system.
  • While ultrasonic transducer 1226 has been described as using the electromagnetic -response of magnetorestrictive materials to produce ultrasonic energy, other arrangements are possible. In some embodiments, acoustic energy in the form of an intense shock wave can be applied directly to process stream 16 using an underwater spark. In some embodiments, ultrasonic energy is transferred to process stream 16 through a thermohydraulic system. For example, acoustic waves of high energy density can be produced by applying power across an enclosed volume of electrolyte, thereby heating the enclosed volume and producing a pressure rise that is subsequently transmitted through a sound propagation medium (e.g., process stream 1216). Design and operation of such a thermohydraulic transducer is discussed in Hartmann et al., U.S. Patent 6,383,152 .
  • Pyrolysis
  • One or more pyrolysis processing sequences can be used to process raw feedstock from a wide variety of different sources to extract useful substances from the feedstock, and to provide partially degraded organic material which functions as input to further processing steps and/or sequences.
  • Referring again to the general schematic in FIG. 8, a first material 2 that includes cellulose having a first number average molecular weight (TMN1) is pyrolyzed, e.g., by heating the first material in a tube furnace, to provide a second material 3 that includes cellulose having a second number average molecular weight (TMN2) lower than the first number average molecular weight. The second material (or the first and second material in certain embodiments) is/are combined with a microorganism (e.g., a bacterium or a yeast) that can utilize the second and/or first material to produce a fuel 5 that is or includes hydrogen, an alcohol (e.g., ethanol or butanol, such as n-, sec or t-butanol), an organic acid, a hydrocarbon or mixtures of any of these.
  • Since the second material has cellulose having a reduced molecular weight relative to the first material, and in some instances, a reduced crystallinity as well, the second material is generally more dispersible, swellable and/or soluble in a solution containing the microorganism, e.g., at a concentration of greater than 106 microorganisms/mL. These properties make the second material 3 more susceptible to chemical, enzymatic and/or microbial attack relative to the first material 2, which can greatly improve the production rate and/or production level of a desired product, e.g., ethanol. Pyrolysis can also sterilize the first and second materials.
  • In some embodiments, the second number average molecular weight ( TMN2 ) is lower than the first number average molecular weight (TMN1) by more than about 10 percent, e.g.,15, 20, 25, 30, 35, 40, 50 percent, 60 percent, or even more than about 75 percent.
  • In some instances, the second material has cellulose that has as crystallinity (TC2) that is lower than the crystallinity (TC1) of the cellulose of the first material. For example, (TC2) can be lower than (TC1) by more than about 10 percent, e.g.,15, 20, 25, 30, 35, 40, or even more than about 50 percent.
  • In some embodiments, the starting crystallinity (prior to pyrolysis) is from about 40 to about 87.5 percent, e.g., from about 50 to about 75 percent or from about 60 to about 70 percent, and the crystallinity index after pyrolysis is from about 10 to about 50 percent, e.g., from about 15 to about 45 percent or from about 20 to about 40 percent. However, in certain embodiments, e.g., after extensive pyrolysis, it is possible to have a crystallinity index of lower than 5 percent. In some embodiments, the material after pyrolysis is substantially amorphous.
  • In some embodiments, the starting number average molecular weight (prior to pyrolysis) is from about 200,000 to about 3,200,000, e.g., from about 250,000 to about 1,000,000 or from about 250,000 to about 700,000, and the number average molecular weight after pyrolysis is from about 50,000 to about 200,000, e.g., from about 60,000 to about 150,000 or from about 70,000 to about 125,000. However, in some embodiments, e.g., after extensive pyrolysis, it is possible to have a number average molecular weight of less than about 10,000 or even less than about 5,000.
  • In some embodiments, the second material can have a level of oxidation (TO2) that is higher than the level of oxidation (TO1) of the first material. A higher level of oxidation of the material can aid in its dispersability, swellability and/or solubility, further enhancing the materials susceptibility to chemical, enzymatic or microbial attack. In some embodiments, to increase the level of the oxidation of the second material relative to the first material, the pyrolysis is performed in an oxidizing environment, producing a second material that is more oxidized than the first material. For example, the second material can have more hydroxyl groups, aldehyde groups, ketone groups, ester groups or carboxylic acid groups, which can increase its hydrophilicity.
  • In some embodiments, the pyrolysis of the materials is continuous. In other embodiments, the material is pyrolyzed for a pro-determined time, and then allowed to cool for a second pre-determined time before pyrolyzing again.
  • Pyrolysis systems
  • FIG. 14 shows a process flow diagram 6000 that includes various steps in a pyrolytic feedstock pretreatment system.. In first step 6010, a supply of dry feedstock is received from a feed source.
  • As described above, the dry feedstock from the feed source may be pre-processed prior to delivery to the pyrolysis chamber. For example, if the feedstock is derived from plant sources, certain portions of the plant material may be removed prior to collection of the plant material and/or before the plant material is delivered by the feedstock transport device. Alternatively, or in addition, the biomass feedstock can be subjected to mechanical processing 6020 (e.g., to reduce the average length of fibers in the feedstock) prior to delivery to the pyrolysis chamber.
  • Following mechanical processing, the feedstock undergoes a moisture adjustment step 6030. The nature of the moisture adjustment step depends upon the moisture content of the mechanically processed feedstock. Typically, pyrolysis of feedstock occurs most efficiently when the moisture content of the feedstock is between about 10% and about 30% (e.g., between 15% and 25%) by weight of the feedstock. If the moisture content of the feedstock is larger than about 40% by weight, the extra thermal load presented by the water content of the feedstock increases the energy consumption of subsequent pyrolysis steps.
  • In some embodiments, if the feedstock has a moisture content which is larger than about 30% by weight, drier feedstock material 6220 which has a low moisture content can be blended in, creating a feedstock mixture in step 6030 with an average moisture content that is within the limits discussed above. In certain embodiments, feedstock with a high moisture content can simply be dried by dispersing the feedstock material on a moving conveyor that cycles the feedstock through an in-line heating unit. The heating unit evaporates a portion of the water present in the feedstock.
  • In some embodiments, if the feedstock from step 6020 has a moisture content which is too low (e.g., lower than about 10% by weight), the mechanically processed feedstock can be combined with wetter feedstock material 6230 with a higher moisture content, such as sewage sludge. Alternatively, or in addition, water 6240 can be added to the dry feedstock from step 6020 to increase its moisture content.
  • In step 6040, the feedstock - now with its moisture content adjusted to fall within suitable limits - can be preheated in an optional preheating step 6040. Preheating step 6040 can be used to increase the temperature of the feedstock to between 75 °C and 150°C in preparation for subsequent pyrolysis of the feedstock. Depending upon the nature of the feedstock and the particular design of the pyrolysis chamber, preheating the feedstock can ensure that heat distribution within the feedstock remains more uniform during pyrolysis, and can reduce the thermal load on the pyrolysis chamber.
  • The feedstock is then transported to a pyrolysis chamber to undergo pyrolysis in step 6050. In some embodiments, transport of the feedstock is assisted by adding one or more pressurized gases 6210 to the feedstock stream. The gases create a pressure gradient in a feedstock transport conduit, propelling the feedstock into the pyrolysis chamber (and even through the pyrolysis chamber). In certain embodiments, transport of the feedstock occurs mechanically; that is, a transport system that includes a conveyor such as an auger transports the feedstock to the pyrolysis chamber.
  • Other gases 6210 can also be added to the feedstock prior to the pyrolysis chamber. In some embodiments, for example, one or more catalyst gases can be added to the feedstock to assist decomposition of the feedstock during pyrolysis. In certain embodiments, one or more scavenging agents can be added to the feedstock to trap volatile materials released during pyrolysis. For example, various sulfur-based compounds such as sulfides can be liberated during pyrolysis, and an agent such as hydrogen gas can be added to the feedstock to cause desulfurization of the pyrolysis products. Hydrogen combines with sulfides to form hydrogen sulfide gas, which can be removed from the pyrolyzed feedstock.
  • Pyrolysis of the feedstock within the chamber can include heating the feedstock to relatively high temperatures to cause partial decomposition of the feedstock. Typically, the feedstock is heated to a temperature in a range from 150 °C to 1100 °C. The temperature to which the feedstock is heated depends upon a number of factors, including the composition of the feedstock, the feedstock average particle size, the moisture content, and the desired pyrolysis products. For many types of biomass feedstock, for example, pyrolysis temperatures between 300 °C and 550 °C are used.
  • The residence time of the feedstock within the pyrolysis chamber generally depends upon a number of factors, including the pyrolysis temperature, the composition of the feedstock, the feedstock average particle size, the moisture content, and the desired pyrolysis products. In some embodiments, feedstock materials are pyrolyzed at a temperature just above the decomposition temperature for the material in an inert atmosphere, e.g., from about 2°C above to about 10 °C above the decomposition temperature or from about 3 °C above to about 7 °C above the decomposition temperature. In such embodiments, the material is generally kept at this temperature for greater than 0.5 hours, e.g., greater than 1.0 hours or greater than about 2.0 hours. In other embodiments, the materials are pyrolyzed at a temperature well above the decomposition temperature for the material in an inert atmosphere, e.g., from about 75 °C above to about 175 °C above the decomposition temperature or from about 85 °C above to about 150 °C above the decomposition temperature. In such embodiments, the material is generally kept at this temperature for less than 0.5 hour, e.g., less 20 minutes, less than 10 minutes, less than 5 minutes or less than 2 minutes. In still other embodiments, the materials are pyrolyzed at an extreme temperature, e.g., from about 200 °C above to about 500 °C above the decomposition temperature of the material in an inert environment or from about 250 °C above to about 400 °C above the decomposition temperature. In such embodiments, the material us generally kept at this temperature for less than 1 minute, e.g., less than 30 seconds, less than 15 seconds, less than 10 seconds, less than 5 seconds, less than 1 second or less than 500 ms. Such embodiments are typically referred to as flash pyrolysis.
  • In some embodiments, the feedstock is heated relatively rapidly to the selected pyrolysis temperature within the chamber. For example, the chamber can be designed to heat the feedstock at a rate of between 500 °C/s and 11,000 °C/s. Typical heating rates for biomass-derived feedstock material are from 500 °C/s to 1000 °C/s, for example.
  • A turbulent flow of feedstock material within the pyrolysis chamber is usually advantageous, as it ensures relatively efficient heat transfer to the feedstock material from the heating sub-system. Turbulent flow can be achieved by blowing the feedstock material through the chamber using one or more injected carrier gases 6210, for example. In general, the carrier gases are relatively inert towards the feedstock material, even at the high temperatures in the pyrolysis chamber. Exemplary carrier gases include, for example, nitrogen, argon, methane, carbon monoxide, and carbon dioxide. Alternatively, or in addition, mechanical transport systems such as augers can transport and circulate the feedstock within the pyrolysis chamber to create a turbulent feedstock flow.
  • In some embodiments, pyrolysis of the feedstock occurs substantially in the absence of oxygen and other reactive gases. Oxygen can be removed from the pyrolysis chamber by periodic purging of the chamber with high pressure nitrogen (e.g., at nitrogen pressures of 2 bar or more). Following purging of the chamber, a gas mixture present in the pyrolysis chamber (e.g., during pyrolysis of the feedstock) can include less than 4 mole% oxygen (e.g., less than 1 mole% oxygen, and even less than 0.5 mole% oxygen). The absence of oxygen ensures that ignition of the feedstock does not occur at the elevated pyrolysis temperatures.
  • In certain embodiments, relatively small amounts of oxygen can be introduced into the feedstock and are present during pyrolysis. This technique is referred to as oxidative pyrolysis. Typically, oxidative pyrolysis occurs in multiple heating stages. For example, in a first heating stage, the feedstock is heated in the presence of oxygen to cause partial oxidation of the feedstock. This stage consumes the available oxygen in the pyrolysis chamber. Then, in subsequent heating stages, the feedstock temperature is further elevated. With all of the oxygen in the chamber consumed, however, feedstock combustion does not occur, and combustion-free pyrolytic decomposition of the feedstock (e.g., to generate hydrocarbon products) occurs. In general, the process of heating feedstock in the pyrolysis chamber to initiate decomposition is endothermic. However, in oxidative pyrolysis, formation of carbon dioxide by oxidation of the feedstock is an exothermic process. The heat released from carbon dioxide formation can assist further pyrolysis heating stages, thereby lessening the thermal load presented by the feedstock.
  • In some embodiments, pyrolysis occurs in an inert environment, such as while feedstock materials are bathed in argon or nitrogen gas. In certain embodiments, pyrolysis can occur in an oxidizing environment, such as in air or argon enriched in air. In some embodiments, pyrolysis can take place in a reducing environment, such as while feedstock materials are bathed in hydrogen gas. To aid pyrolysis, various chemical agents, such as oxidants, reductants, acids or bases can be added to the material prior to or during pyrolysis. For example, sulfuric acid can be added, or a peroxide (e.g., benzoyl peroxide) can be added.
  • As discussed above, a variety of different processing conditions can be used, depending upon factors such as the feedstock composition and the desired pyrolysis products. For example, for cellulose-containing feedstock material, relatively mild pyrolysis conditions can be employed, including flash pyrolysis temperatures between 375 °C and 450 °C, and residence times of less than 1 second. As another example, for organic solid waste material such as sewage sludge, flash pyrolysis temperatures between 500 °C and 650°C are typically used, with residence times of between 0.5 and 3 seconds. In general, many of the pyrolysis process parameters, including residence time, pyrolysis temperature, feedstock turbulence, moisture content, feedstock composition, pyrolysis product composition, and additive gas composition can be regulated automatically by a system of regulators and an automated control system.
  • Following pyrolysis step 6050, the pyrolysis products undergo a quenching step 6250 to reduce the temperature of the products prior to further processing. Typically, quenching step 6250 includes spraying the pyrolysis products with streams of cooling water 6260. The cooling water also forms a slurry that includes solid, undissolved product material and various dissolved products. Also present in the product stream is a mixture that includes various gases, including product gases, carrier gases, and other types of process gases.
  • The product stream is transported via in-line piping to a gas separator that performs a gas separation step 6060, in which product gases and other gases are separated from the slurry formed by quenching the pyrolysis products. The separated gas mixture is optionally directed to a blower 6130, which increases the gas pressure by blowing air into the mixture. The gas mixture can be subjected to a filtration step 6140, in which the gas mixture passes through one or more filters (e.g., activated charcoal filters) to remove particulates and other impurities. In a subsequent step 6150, the filtered gas can be compressed and stored for further use. Alternatively, the filtered gas can be subjected to further processing steps 6160. For example, in some embodiments, the filtered gas can be condensed to separate different gaseous compounds within the gas mixture. The different compounds can include, for example, various hydrocarbon products (e.g., alcohols, alkanes, alkenes, alkynes, ethers) produced during pyrolysis. In certain embodiments, the filtered gas containing a mixture of hydrocarbon components can be combined with steam gas 6170 (e.g., a mixture of water vapor and oxygen) and subjected to a cracking process to reduce molecular weights of the hydrocarbon components.
  • In some embodiments, the pyrolysis chamber includes heat sources that burn hydrocarbon gases such as methane, propane, and/or butane to heat the feedstock. A portion 6270 of the separated gases can be recirculated into the pyrolysis chamber for combustion, to generate process heat to sustain the pyrolysis process.
  • In certain embodiments, the pyrolysis chamber can receive process heat that can be used to increase the temperature of feedstock materials. For example, irradiating feedstock with radiation (e.g., gamma radiation, electron beam radiation, or other types of radiation) can heat the feedstock materials to relatively high temperatures. The heated feedstock materials can be cooled by a beat exchange system that removes some of the excess heat from the irradiated feedstock. The heat exchange system can be configured to transport some of the heat energy to the pyrolysis chamber to heat (or pre-heat) feedstock material, thereby reducing energy cost for the pyrolysis process.
  • The slurry containing liquid and solid pyrolysis products can undergo an optional dewatering step 6070, in which excess water can be removed from the slurry via processes such as mechanical pressing and evaporation. The excess water 6280 can be filtered and then recirculated for further use in quenching the pyrolysis decomposition products in step 6250.
  • The de-watered slurry then undergoes a mechanical separation step 6080, in which solid product material 6110 is separated from liquid product material 6090 by a series of increasingly-fine filters. In step 6100, the liquid product material 6090 can then be condensed (e.g., via evaporation) to remove waste water 6190, and purified by processes such as extraction. Extraction can include the addition of one or more organic solvents 6180, for example, to separate products such as oils from products such as alcohols. Suitable organic solvents include, for example, various hydrocarbons and halo-hydrocarbons. The purified liquid products 6200 can then be subjected to further processing steps. Waste water 6190 can be filtered if necessary, and recirculated for further use in quenching the pyrolysis decomposition products in step 6250.
  • After separation in step 6080, the solid product material 6110 is optionally subjected to a drying step 6120 that can include evaporation of water. Solid material 6110 can then be stored for later use, or subjected to further processing steps, as appropriate.
  • The pyrolysis process parameters discussed above are exemplary. In general, values of these parameters can vary widely according to the nature of the feedstock and the desired products. Moreover, a wide variety of different pyrolysis techniques, including using heat sources such as hydrocarbon flames and/or furnaces, infrared lasers, microwave heaters, induction heaters, resistive heaters, and other heating devices and configurations can be used.
  • A wide variety of different pyrolysis chambers can be used to decompose the feedstock. In some embodiments, for example, pyrolyzing feedstock can include heating the material using a resistive heating member, such as a metal filament or metal ribbon. The heating can occur by direct contact between the resistive heating member and the material.
  • In certain embodiments, pyrolyzing can include heating the material by induction, such as by using a Currie-Point pyrolyzer. In some embodiments, pyrolyzing can include heating the material by the application of radiation, such as infrared radiation. The radiation can be generated by a laser, such as an infrared laser.
  • In certain embodiments, pyrolyzing can include heating the material with a convective heat. The convective heat can be generated by a flowing stream of heated gas. The heated gas can be maintained at a temperature of less than about 1200 °C, such as less than 1000 °C, less than 750 °C, less than 600 °C, less than 400 °C or even less than 300 °C. The heated gas can be maintained at a temperature of greater than about 250 °C. The convective heat can be generated by a hot body surrounding the first material, such as in a furnace.
  • In some embodiments, pyrolyzing can include heating the material with steam at a temperature above about 250 °C.
  • An embodiment of a pyrolysis chamber is shown in FIG. 15. Chamber 6500 includes an insulated chamber wall 6510 with a vent 6600 for exhaust gases, a plurality of burners 6520 that generate heat for the pyrolysis process, a transport duct 6530 for transporting the feedstock through chamber 6500, augers 6590 for moving the feedstock through duct 6530 in a turbulent flow, and a quenching system 6540 that includes an auger 6610 for moving the pyrolysis products, water jets 6550 for spraying the pyrolysis products with cooling water, and a gas separator for separating gaseous products 6580 from a slurry 6570 containing solid and liquid products.
  • Another embodiment of a pyrolysis chamber is shown in FIG. 16. Chamber 6700 includes an insulated chamber wall 6710, a feedstock supply duct 6720, a sloped inner chamber wall 6730, burners 6740 that generate heat for the pyrolysis process, a vent 6750 for exhaust gases, and a gas separator 6760 for separating gaseous products 6770 from liquid and solid products 6780. Chamber 6700 is configured to rotate in the direction shown by arrow 6790 to ensure adequate mixing and turbulent flow of the feedstock within the chamber.
  • A further embodiment of a pyrolysis chamber is shown in FIG. 17. Filament pyrolyzer 1712 includes a sample holder 1713 with resistive heating element 1714 in the form of a wire winding through the open space defined by the sample holder 1713. Optionally, the heated element can be spun about axis 1715 (as indicated by arrow 1716) to tumble the material that includes the cellulosic material in sample holder 1713. The space 1718 defined by enclosure 1719 is maintained at a temperature above room temperature, e.g., 200 to 250°C. In a typical usage, a carrier gas, e.g., an inert gas, or an oxidizing or reducing gas, traverses through the sample holder 1713 while the resistive heating element is rotated and heated to a desired temperature, e.g., 325°C. After an appropriate time, e.g., 5 to 10 minutes, the pyrolyzed material is emptied from the sample holder. The system shown in FIG. 17 can be scaled and made continuous. For example, rather than a wire as the heating member, the heating member can be an auger screw. Material can continuously fall into the sample holder, striking a heated screw that pyrolizes the material. At the same time, the screw can push the pyrolyzed material out of the sample holder to allow for the entry of fresh, unpyrolyzed material.
  • Another embodiment of a pyrolysis chamber is shown in FIG. 18, which features a Curie-Point pyrolyzer 1820 that includes a sample chamber 1821 housing a ferromagnetic foil 1822. Surrounding the sample chamber 1821 is an RF coil 1823. The space 1824 defined by enclosure 1825 is maintained at a temperature above room temperature, e.g., 200 to 250°C. In a typical usage, a carrier gas traverses through the sample chamber 1821 while the foil 1822 is inductively heated by an applied RF field to pyrolize the material at a desired temperature.
  • Yet another embodiment of a pyrolysis chamber is shown in FIG. 19. Furnace pyrolyzer 130 includes a movable sample holder 131 and a furnace 132. In a typical usage, the sample is lowered (as indicated by arrow 137) into a hot zone 135 of furnace 132, while a carrier gas fills the housing 136 and traverses through the sample holder 131. The sample is heated to the desired temperature for a desired time to provide a pyrolyzed product. The pyrolyzed product is removed from the pyrolyzer by raising the sample holder (as indicated by arrow 134).
  • In certain embodiments, as shown in FIG. 20, a cellulosic target 140 can be pyrolyzed by treating the target, which is housed in a vacuum chamber 141, with laser light, e.g., light having a wavelength of from about 225 nm to about 1500 nm. For example, the target can be ablated at 266 nm, using the fourth harmonic of a Nd-YAG laser (Spectra Physics, GCR170, San Jose, Calif.). The optical configuration shown allows the nearly monochromatic light 143 generated by the laser 142 to be directed using mirrors 144 and 145 onto the target after passing though a lens 146 in the vacuum chamber 141. Typically, the pressure in the vacuum chamber is maintained at less than about 10-6 mm Hg. In some embodiments, infrared radiation is used, e.g., 1.06 micron radiation from a Nd-YAG laser. In such embodiments, a infrared sensitive dye can be combined with the cellulosic material to produce a cellulosic target. The infrared dye can enhance the heating of the cellulosic material. Laser ablation is described by Blanchet-Fincher et al. in U.S. Patent No. 5,942,649 .
  • Referring to FIG. 21, in some embodiments, a cellulosic material can be flash pyrolyzed by coating a tungsten filament 150, such as a 5 to 25 mil tungsten filament, with the desired cellulosic material while the material is housed in a vacuum chamber 151. To affect pyrolysis, current is passed through the filament, which causes a rapid heating of the filament for a desired time. Typically, the heating is continued for seconds before allowing the filament to cool. In some embodiments, the heating is performed a number of times to effect the desired amount of pyrolysis.
  • In certain embodiments, carbohydrate-containing biomass material can be heated in an absence of oxygen in a fluidized bed reactor. If desired, the carbohydrate containing biomass can have relatively thin cross-sections, and can include any of the fibrous materials described herein, for efficient heat transfer. The material can be heated by thermal transfer from a hot metal or ceramic, such as glass beads or sand in the reactor, and the resulting pyrolysis liquid or oil can be transported to a central refinery for making combustible fuels or other useful products.
  • Oxidation
  • One or more oxidative processing sequences can be used to process raw feedstock from a wide variety of different sources to extract useful substances from the feedstock, and to provide partially degraded organic material which functions as input to further processing steps and/or sequences.
  • Referring again to FIG. 8, a first material 2 that includes cellulose having a first number average molecular weight (TMN1) and having a first oxygen content (TO1) is oxidized, e.g., by heating the first material in a tube furnace in stream of air or oxygen-enriched air, to provide a second material 3 that includes cellulose having a second number average molecular weight (TMN2) and having a second oxygen content (TO2) higher than the first oxygen content (TO1). The second material (or the first and second material in certain embodiments) can be, e.g., combined with a resin, such as a molten thermoplastic resin or a microorganism, to provide a composite 4 having desirable mechanical properties, or a fuel 5. Providing a higher level of oxidation can improve dispersability of the oxidized material in a resin and can also improve the interfacial bond between the oxidized material and the resin. Improved dispersability and/or interfacial bonding (in some instances in combination with maintaining molecular weight) can provide composites with exceptional mechanical properties, such as improved abrasion resistance, compression strength, fracture resistance, impact strength, bending strength, tensile modulus, flexural modulus and elongation at break.
  • Such materials can also be combined with a solid and/or a liquid. For example, the liquid can be in the form of a solution and the solid can be particulate in form. The liquid and/or solid can include a microorganism, e.g.; a bacterium, and/or an enzyme. For example, the bacterium and/or enzyme can work on the cellulosic or lignocellulosic material to produce a fuel, such as ethanol, or a coproduct, such as a protein. Fuels and coproducts are described in FIBROUS MATERIALS AND COMPOSITES," USSN 11/453,951, filed June 15, 2006 .. The entire contents of each of the foregoing applications are incorporated herein by reference.
  • In some embodiments, the second number average molecular weight is not more 97 percent lower than the first number average molecular weight, e.g., not more than 95 percent, 90, 85, 80, 75, 70, 65, 60, 55, 50, 45, 40, 30, 20,12.5,10.0, 7.5, 5.0, 4.0, 3.0, 2.5, 2.0 or not more than 1.0 percent lower than the first number average molecular weight. The amount of reduction of molecular weight will depend upon the application. For example, in some preferred embodiments that provide composites, the second number average molecular weight is substantially the same as the first number average molecular weight. In other applications, such as making ethanol or another fuel or coproduct, a higher amount of molecular weight reduction is generally preferred.
  • For example, in some embodiments that provide a composite, the starting number average molecular weight (prior to oxidation) is from about 200,000 to about 3,200,000, e.g., from about 250,000 to about 1,000,000 or from about 250,000 to about 700,000, and the number average molecular weight after oxidation is from about 175,000 to about 3,000,000, e.g., from about 200,000 to about 750,000 or from about 225,000 to about 600,000.
  • Resins utilized can be thermosets or thermoplastics. Examples of thermoplastic resins include rigid and elastomeric thermoplastics. Rigid thermoplastics include polyolefins (e.g., polyethylene, polypropylene, or polyolefin copolymers), polyesters (e.g., polyethylene terephthalate), polyamides (e.g., nylon 6,6/12 or 6/10), and polyethyleneimines. Examples of elastomeric thermoplastic resins include elastomeric styrenic copolymers (e.g., styrene-ethylene-butylene-styrene copolymers), polyamide elastomers (e.g., polyether-polyamide copolymers) and ethylene-vinyl acetate copolymer.
  • In particular embodiments, lignin is utilized, e.g., any lignin that is generated in any process described herein.
  • In some embodiments, the thermoplastic resin has a melt flow rate of between 10 g/10 minutes to 60 g/10 minutes, e.g., between 20 g/10 minutes to 50 g/10 minutes, or between 30 g/10 minutes to 45 g/10 minutes, as measured using ASTM 1238. In certain embodiments, compatible blends of any of the above thermoplastic resins can be used.
  • In some embodiments, the thermoplastic resin has a polydispersity index (PDI), i.e., a ratio of the weight average molecular weight to the number average molecular weight, of greater than 1.5, e.g., greater than 2.0, greater than 2.5, greater than 5.0, greater than 7.5, or even greater than 10.0.
  • In specific embodiments, polyolefins or blends of polyolefins are utilized as the thermoplastic resin.
  • Examples of thermosetting resins include natural rubber, butadiene-rubber and polyurethanes.
  • In some embodiments in which the materials are used to make a fuel or a coproduct, the starting number average molecular weight (prior to oxidation) is from about 200,000 to about 3,200,000, e.g., from about 250,000 to about 1,000,000 or from about 250,000 to about 700,000, and the number average molecular weight after oxidation is from about 50,000 to about 200,000, e.g., from about 60,000 to about 150,000 or from about 70,000 to about 125,000. However, in some embodiments, e.g., after extensive oxidation, it is possible to have a number average molecular weight of less than about 10,000 or even less than about 5,000.
  • In some embodiments, the second oxygen content is at least about five percent higher than the first oxygen content, e.g., 7.5 percent higher, 10.0 percent higher, 12.5 percent higher, 15.0 percent higher or 17.5 percent higher. In some preferred embodiments, the second oxygen content is at least about 20.0 percent higher than the oxygen content of the first material. Oxygen content is measured by elemental analysis by pyrolyzing a sample in a furnace operating 1300 °C or higher. A suitable elemental analyzer is the LECO CHNS-932 analyzer with a VTF-900 high temperature pyrolysis furnace.
  • In some embodiments, oxidation of first material 200 does not result in a substantial change in the crystallinity of the cellulose. However, in some instances, e.g., after extreme oxidation, the second material has cellulose that has as crystallinity (TC2) that is lower than the crystallinity (TC1) of the cellulose of the first material. For example, (TC2) can be lower than (TC1) by more than about 5 percent, e.g., 10, 15, 20, or even 25 percent. This can be desirable when optimizing the flexural fatigue properties of the composite is a goal. For example, reducing the crystallinity can improve the elongation at break or can enhance the impact resistance of a composite. This can also be desirable to enhance solubility of the materials in a liquid, such as a liquid that includes a bacterium and/or an enzyme.
  • In some embodiments, the starting crystallinity index (prior to oxidation) is from about 40 to about 87.5 percent, e.g., from about 50 to about 75 percent or from about 60 to about 70 percent, and the crystallinity index after oxidation is from about 30 to about 75.0 percent, e.g., from about 35.0 to about 70.0 percent or from about 37.5 to about 65.0 percent. However, in certain embodiments, e.g., after extensive oxidation, it is possible to have a crystallinity index of lower than 5 percent. In some embodiments, the material after oxidation is substantially amorphous.
  • Without wishing to be bound by any particular theory, it is believed that oxidation increases the number of hydrogen-bonding groups on the cellulose, such as hydroxyl groups, aldehyde groups, ketone groups carboxylic acid groups or anhydride groups, which can increase its dispersability and/or its solubility (e.g., in a liquid). To further improve dispersability in a resin, the resin can include a component that includes hydrogen-bonding groups, such as one or more anhydride groups, carboxylic acid groups, hydroxyl groups, amide groups, amine groups or mixtures of any of these groups. In some preferred embodiments, the component includes a polymer copolymerized with and/or grafted with maleic anhydride. Such materials are available from Dupont under the tradename FUSABOND®.
  • Generally, oxidation of first material 200 occurs in an oxidizing environment. For example, the oxidation can be effected or aided by pyrolysis in an oxidizing environment, such as in air or argon enriched in air. To aid in the oxidation, various chemical agents, such as oxidants, acids or bases can be added to the material prior to or during oxidation. For example, a peroxide (e.g., benzoyl peroxide) can be added prior to oxidation.
  • Oxidation Systems
  • FIG. 22 shows a process flow diagram 5000 that includes various steps in an oxidative feedstock pretreatment system. In first step 5010, a supply of dry feedstock is received from a feed source. The feed source can include, for example, a storage bed or container that is connected to an in-line oxidation reactor via a conveyor belt or another feedstock transport device.
  • As described above, the dry feedstock from the feed source may be pre-processed prior to delivery to the oxidation reactor. For example, if the feedstock is derived from plant sources, certain portions of the plant material may be removed prior to collection of the plant material and/or before the plant material is delivered by the feedstock transport device. Alternatively, or in addition, the biomass feedstock can be subjected to mechanical processing (e.g., to reduce the average length of fibers in the feedstock) prior to delivery to the oxidation reactor.
  • Following mechanical processing 5020, feedstock 5030 is transported to a mixing system which introduces water 5150 into the feedstock in a mechanical mixing process. Combining water with the processed feedstock in mixing step 5040 creates an aqueous feedstock slurry 5050 which can then be treated with one or more oxidizing agents.
  • Typically, one liter of water is added to the mixture for every 0.02 kg to 1.0 kg of dry feedstock. The ratio of feedstock to water in the mixture depends upon the source of the feedstock and the specific oxidizing agents used further downstream in the overall process. For example, in typical industrial processing sequences for lignocellulosic biomass, aqueous feedstock slurry 5050 includes from about 0.5 kg to about 1.0 kg of dry biomass per liter of water.
  • In some embodiments, one or more fiber-protecting additives 5170 can also be added to the feedstock slurry in feedstock mixing step 5040. Fiber-protecting additives help to reduce degradation of certain types of biomass fibers (e.g., cellulose fibers) during oxidation of the feedstock. Fiber-protecting additives can be used, for example, if a desired product from processing a lignocellulosic feedstock includes cellulose fibers. Exemplary fiber-protecting additives include magnesium compounds such as magnesium hydroxide. Concentrations of fiber-protecting additives in feedstock slurry 5050 can be from 0.1% to 0.4% of the dry weight of the biomass feedstock, for example.
  • In certain embodiments, aqueous feedstock slurry 5050 can be subjected to an optional extraction 5180 with an organic solvent to remove water-insoluble substances from the slurry. For example, extraction of slurry 5050 with one or more organic solvents yields a purified slurry and an organic waste stream 5210 that includes water-insoluble materials such as fats, oils, and other non-polar, hydrocarbon-based substances. Suitable solvents for performing extraction of slurry 5050 include various alcohols, hydrocarbons, and halo-hydrocarbons, for example.
  • In some embodiments, aqueous feedstock slurry 5050 can be subjected to an optional thermal treatment 5190 to further prepare the feedstock for oxidation. An example of a thermal treatment includes heating the feedstock slurry in the presence of pressurized steam. In fibrous biomass feedstock, the pressurized steam swells the fibers, exposing a larger fraction of fiber surfaces to the aqueous solvent and to oxidizing agents that are introduced in subsequent processing steps.
  • In certain embodiments, aqueous feedstock slurry 5050 can be subjected to an optional treatment with basic agents 5200. Treatment with one or more basic agents can help to separate lignin from cellulose in lignocellulosic biomass feedstock, thereby improving subsequent oxidation of the feedstock. Exemplary basic agents include alkali and alkaline earth hydroxides such as sodium hydroxide, potassium hydroxide, and calcium hydroxide. In general, a variety of basic agents can be used, typically in concentrations from about 0.01% to about 0.5% of the dry weight of the feedstock.
  • Aqueous feedstock slurry 5050 is transported (e.g., by an in-line piping system) to a chamber, which can be an oxidation preprocessing chamber or an oxidation reactor. In oxidation preprocessing step 5060, one or more oxidizing agents 5160 are added to feedstock slurry 5050 to form an oxidizing medium. In some embodiments, for example, oxidizing agents 5160 can include hydrogen peroxide. Hydrogen peroxide can be added to slurry 5050 as an aqueous solution, and in proportions ranging from 3% to between 30% and 35% by weight of slurry 5050. Hydrogen peroxide has a number of advantages as an oxidizing agent For example, aqueous hydrogen peroxide solution is relatively inexpensive, is relatively chemically stable, is not particularly hazardous relative to other oxidizing agents (and therefore does not require burdensome handling procedures and expensive safety equipment). Moreover, hydrogen peroxide decomposes to form water during oxidation of feedstock, so that waste stream cleanup is relatively straightforward and inexpensive.
  • In certain embodiments, oxidizing agents 5160 can include oxygen (e.g., oxygen gas) either alone, or in combination with hydrogen peroxide. Oxygen gas can be bubbled into slurry 5050 in proportions ranging from 0.5% to 10% by weight of slurry 5050. Alternatively, or in addition, oxygen gas can also be introduced into a gaseous phase in equilibrium with slurry 5050 (e.g., a vapor head above slurry 5050). The oxygen gas can be introduced into either an oxidation preprocessing chamber or into an oxidation reactor (or into both), depending upon the configuration of the oxidative processing system. Typically, for example, the partial pressure of oxygen in the vapor above slurry 5050 is larger than the ambient pressure of oxygen, and ranges from 0.5 bar to 35 bar, depending upon the nature of the feedstock.
  • The oxygen gas can be introduced in pure form, or can be mixed with one or more carrier gases. For example, in some embodiments, high-pressure air provides the oxygen in the vapor. In certain embodiments, oxygen gas can be supplied continuously to the vapor phase to ensure that a concentration of oxygen in the vapor remains within certain predetermined limits during processing of the feedstock. In some embodiments, oxygen gas can be introduced initially in sufficient concentration to oxidize the feedstock, and then the feedstock can be transported to a closed, pressurized vessel (e.g., an oxidation reactor) for processing.
  • In certain embodiments, oxidizing agents 5160 can include nascent oxygen (e.g., oxygen radicals). Typically, nascent oxygen is produced as needed in an oxidation reactor or in a chamber in fluid communication with an oxidation reactor by one or more decomposition reactions. For example, in some embodiments, nascent oxygen can be produced from a reaction between NO and O2 in a gas mixture or in solution. In certain embodiments, nascent oxygen can be produced from decomposition of HOCl in solution. Other methods by which nascent oxygen can be produced include via electrochemical generation in electrolyte solution, for example.
  • In general, nascent oxygen is an efficient oxidizing agent due to the relatively high reactivity of the oxygen radical. However, nascent oxygen can also be a relatively selective oxidizing agent. For example, when lignocellulosic feedstock is treated with nascent oxygen, selective oxidation of lignin occurs in preference to the other components of the feedstock such as cellulose. As a result, oxidation of feedstock with nascent oxygen provides a method for selective removal of the lignin fraction in certain feedstocks. Typically, nascent oxygen concentrations of between about 0.5% and 5% of the dry weight of the feedstock are used to effect efficient oxidation.
  • Without wishing to be bound by theory, it is believed that nascent oxygen reacts with lignocellulosic feedstock according to at least two different mechanisms. In a first mechanism, nascent oxygen undergoes an addition reaction with the lignin, resulting in partial oxidation of the lignin, which solubilizes the lignin in aqueous solution. As a result, the solubilized lignin can be removed from the rest of the feedstock via washing. In a second mechanism, nascent oxygen disrupts butane cross-links and/or opens aromatic rings that are connected via the butane cross-links. As a result, solubility of the lignin in aqueous solution increases, and the lignin fraction can be separated from the remainder of the feedstock via washing.
  • In some embodiments, oxidizing agents 5160 include ozone (O3). The use of ozone can introduce several chemical handling considerations in the oxidation processing sequence. If heated too vigorously, an aqueous solution of ozone can decompose violently, with potentially adverse consequences for both human system operators and system equipment. Accordingly, ozone is typically generated in a thermally isolated, thick-walled vessel separate from the vessel that contains the feedstock slurry, and transported thereto at the appropriate process stage.
  • Without wishing to be bound by theory, it is believed that ozone decomposes into oxygen and oxygen radicals, and that the oxygen radicals (e.g., nascent oxygen) are responsible for the oxidizing properties of ozone in the manner discussed above. Ozone typically preferentially oxidizes the lignin fraction in lignocellulosic materials, leaving the cellulose fraction relatively undisturbed.
  • Conditions for ozone-based oxidation of biomass feedstock generally depend upon the nature of the biomass. For example, for cellulosic and/or lignocellulosic feedstocks, ozone concentrations of from 0.1 g/m3 to 20 g/m3 of dry feedstock provide for efficient feedstock oxidation. Typically, the water content in slurry 5050 is between 10% by weight and 80% by weight (e.g., between 40% by weight and 60% by weight). During ozone-based oxidation, the temperature of slurry 5050 can be maintained between 0°C and 100 °C to avoid violent decomposition of the ozone.
  • In some embodiments, feedstock slurry 5050 can be treated with an aqueous, alkaline solution that includes one or more alkali and alkaline earth hydroxides such as sodium hydroxide, potassium hydroxide, and calcium hydroxide, and then treated thereafter with an ozone-containing gas in an oxidation reactor. This process has been observed to significantly increase decomposition of the biomass in slurry 5050. Typically, for example, a concentration of hydroxide ions in the alkaline solution is between 0.001% and 10% by weight of slurry 5050. After the feedstock has been wetted via contact with the alkaline solution, the ozone-containing gas is introduced into the oxidation reactor, where it contacts and oxidizes the feedstock.
  • Oxidizing agents 5160 can also include other substances. In some embodiments, for example, halogen-based oxidizing agents such as chlorine and oxychlorine agents (e.g., hypochlorite) can be introduced into slurry 5050. In certain embodiments, nitrogen-containing oxidizing substances can be introduced into slurry 5050. Exemplary nitrogen-containing oxidizing substances include NO and NO2, for example. Nitrogen-containing agents can also be combined with oxygen in slurry 5050 to create additional oxidizing agents. For example, NO and NO2 both combine with oxygen in slurry 5050 to form nitrate compounds, which are effective oxidizing agents for biomass feedstock. Halogen- and nitrogen-based oxidizing agents can, in some embodiments, cause bleaching of the biomass feedstock, depending upon the nature of the feedstock. The bleaching may be desirable for certain biomass-derived products that are extracted in subsequent processing steps.
  • Other oxidizing agents can include, for example, various peroxyacids, peroxyacetic acids, persulfates, percarbonates, permanganates, osmium tetroxide, and chromium oxides.
  • Following oxidation preprocessing step 5060, feedstock slurry 5050 is oxidized in step 5070. If oxidizing agents 5160 were added to slurry 5050 in an oxidation reactor, then oxidation proceeds in the same reactor. Alternatively, if oxidizing agents 5160 were added to slurry 5050 in a preprocessing chamber, then slurry 5050 is transported to an oxidation reactor via an in-line piping system. Once inside the oxidation reactor, oxidation of the biomass feedstock proceeds under a controlled set of environmental conditions. Typically, for example, the oxidation reactor is a cylindrical vessel that is closed to the external environment and pressurized. Both batch and continuous operation is possible, although environmental conditions are typically easier to control in in-line batch processing operations.
  • Oxidation of feedstock slurry 5050 typically occurs at elevated temperatures in the oxidation reactor. For example, the temperature of slurry 5050 in the oxidation reactor is typically maintained above 100°C, in a range from 120°C to 240°C. For many types of biomass feedstock, oxidation is particularly efficient if the temperature of slurry 5050 is maintained between 150°C and 220 °C. Slurry 5050 can be heating using a variety of thermal transfer devices. For example, in some embodiments, the oxidation reactor contacts a heating bath that includes oil or molten salts, In certain embodiments, a series of heat exchange pipes surround and contact the oxidation reactor, and circulation of hot fluid within the pipes heats slurry 5050 in the reactor. Other heating devices that can be used to heat slurry 5050 include resistive heating elements, induction heaters, and microwave sources, for example.
  • The residence time of feedstock slurry 5050 in the oxidation reactor can be varied as desired to process the feedstock. Typically, slurry 5050 spends from 1 minute to 60 minutes undergoing oxidation in the reactor. For relatively soft biomass material such as lignocellulosic matter, the residence time in the oxidation reactor can be from 5 minutes to 30 minutes, for example, at an oxygen pressure of between 3 and 12 bars in the reactor, and at a slurry temperature of between 160°C and 210 °C. For other types of feedstock, however, residence times in the oxidation reactor can be longer, e.g., as long 48 hours. To determine appropriate residence times for slurry 5050 in the oxidation reactor, aliquots of the slurry can be extracted from the reactor at specific intervals and analyzed to determine concentrations of particular products of interest such as complex saccharides. Information about the increase in concentrations of certain products in slurry 5050 as a function of time can be used to determine residence times for particular classes of feedstock material.
  • In some embodiments, during oxidation of feedstock slurry 5050, adjustment of the slurry pH may be performed by introducing one or more chemical agents into the oxidation reactor. For example, in certain embodiments, oxidation occurs most efficiently in a pH range of about 9-11. To maintain a pH in this range, agents such as alkali and alkaline earth hydroxides, carbonates, ammonia, and alkaline buffer solutions can be introduced into the oxidation reactor.
  • Circulation of slurry 5050 during oxidation can be important to ensure sufficient contact between oxidizing agents 5160 and the feedstock. Circulation of the slurry can be achieved using a variety of techniques. For example, in some embodiments, a mechanical stirring apparatus that includes impeller blades or a paddle wheel can be implemented in the oxidation reactor. In certain embodiments, the oxidation reactor can be a loop reactor, in which the aqueous solvent in which the feedstock is suspended is simultaneously drained from the bottom of the reactor and recirculated into the top of the reactor via pumping, thereby ensuring that the slurry is continually re-mixed and does not stagnate within the reactor.
  • After oxidation of the feedstock is complete, the slurry is transported to a separation apparatus where a mechanical separation step 5080 occurs. Typically, mechanical separation step 5080 includes one or more stages of increasingly-fine filtering of the slurry to mechanically separate the solid and liquid constituents.
  • Liquid phase 5090 is separated from solid phase 5100, and the two phases are processed independently thereafter. Solid phase 5100 can optionally undergo a drying step 5120 in a drying apparatus, for example. Drying step 5120 can include, for example, mechanically dispersing the solid material onto a drying surface, and evaporating water from solid phase 5100 by gentle heating of the solid material. Following drying step 5120 (or, alternatively, without undergoing drying step 5120), solid phase 5100 is transported for further processing steps 5140.
  • Liquid phase 5090 can optionally undergo a drying step 5110 to reduce the concentration of water in the liquid phase. In some embodiments, for example, drying step 5110 can include evaporation and/or distillation and/or extraction of water from liquid phase 5090 by gentle heating of the liquid. Alternatively, or in addition, one or more chemical drying agents can be used to remove water from liquid phase 5090. Following drying step 5110 (or alternatively, without undergoing drying step 5110), liquid phase 5090 is transported for further processing steps 5130, which can include a variety of chemical and biological treatment steps such as chemical and/or enzymatic hydrolysis.
  • Drying step 5110 creates waste stream 5220, an aqueous solution that can include dissolved chemical agents such as acids and bases in relatively low concentrations. Treatment of waste stream 5220 can include, for example, pH neutralization with one or more mineral acids or bases. Depending upon the concentration of dissolved salts in waste stream 5220, the solution may be partially de-ionized (e.g., by passing the waste stream through an ion exchange system). Then, the waste stream - which includes primarily water - can be re-circulated into the overall process (e.g., as water 5150), diverted to another process, or discharged.
  • Typically, for lignocellulosic biomass feedstocks following separation step 5070, liquid phase 5090 includes a variety of soluble poly- and oligosaccharides, which can then be separated and/or reduced to smaller-chain saccharides via further processing steps. Solid phase 5100 typically includes primarily cellulose, for example, with smaller amounts of hemicellulose- and lignin-derived products.
  • In some embodiments, oxidation can be carried out at elevated temperature in a reactor such as a pyrolysis chamber. For example, referring again to FIG. 17, feedstock materials can be oxidized in filament pyrolyzer 1712. In a typical usage, an oxidizing carrier gas, e.g., air or an air/argon blend, traverses through the sample holder 1713 while the resistive heating element is rotated and heated to a desired temperature, e.g., 325 °C. After an appropriate time, e.g., 5 to 10 minutes, the oxidized material is emptied from the sample holder. The system shown in FIG. 2 can be scaled and made continuous. For example, rather than a wire as the heating member, the heating member can be an auger screw. Material can continuously fall into the sample holder, striking a heated screw that pyrolizes the material. At the same time, the screw can push the oxidized material out of the sample holder to allow for the entry of fresh, unoxidized material.
  • Referring again to FIG. 18, feedstock materials can be oxidized in a Curie-Point pyrolyzer 1820. In a typical usage, an oxidizing carrier gas traverses through the sample chamber 1821 while the foil 1822 is inductively heated by an applied RF field to oxidize the material at a desired temperature.
  • Referring again to FIG. 19, feedstock materials can be oxidized in a furnace pyrolyzer 130. In a typical usage, the sample is lowered (as indicated by arrow 137) into a hot zone 135 of furnace 132, while an oxidizing carrier gas fills the housing 136 and traverses through the sample holder 131. The sample is heated to the desired temperature for a desired time to provide an oxidized product. The oxidized product is removed from the pyrolyzer by raising the sample holder (as indicated by arrow 134).
  • Referring again to FIG. 20, feedstock materials can be oxidized by forming a cellulosic target 140, along with an oxidant, such as a peroxide, and treating the target, which is housed in a vacuum chamber 141, with laser light, e.g., light having a wavelength of from about 225 nm to about 1600 nm. The optical configuration shown allows the monochromatic light 143 generated by the laser 142 to be directed using mirrors 144 and 145 onto the target after passing though a lens 146 in the vacuum chamber 141. Typically, the pressure in the vacuum chamber is maintained at less than about 10-6 mm Hg. In some embodiments, infrared radiation is used, e.g., 1.06 micron radiation from a Nd-YAG laser. In such embodiments, a infrared sensitive dye can be combined with the cellulosic material to produce a cellulosic target. The infrared dye can enhance the heating of the cellulosic material. Laser treatment of polymers is described by Blanchet-Fincher et al. in U.S. Patent No. 5,942,649 .
  • Referring again to FIG. 21, feedstock materials can be rapidly oxidized by coating a tungsten filament 150, together with an oxidant, such as a peroxide, with the desired cellulosic material while the material is housed in a vacuum chamber 151. To affect oxidation, current is passed through the filament, which causes a rapid heating of the filament for a desired time. Typically, the heating is continued for seconds before allowing the filament to cool. In some embodiments, the heating is performed a number of times to effect the desired amount of oxidation.
  • Referring again to FIG. 12, in some embodiments, feedstock materials can be oxidized with the aid of sound and/or cavitation. Generally, to effect oxidation, the materials are sonicated in an oxidizing environment, such as water saturated with oxygen or another chemical oxidant, such as hydrogen peroxide.
  • Referring again to FIGS. 9 and 10, in certain embodiments, ionizing radiation is used to aid in the oxidation of feedstock materials. Generally, to effect oxidation, the materials are irradiated in an oxidizing environment, such as air or oxygen. For example, gamma radiation and/or electron beam radiation can be employed to irradiate the materials.
  • Other Processes
  • Steam explosion can be used alone without any of the processes described herein, or in combination with any of the processes described herein.
  • FIG 23 shows an overview of the entire process of converting a fiber source 400 into a product 450, such as ethanol, by a process that includes shearing and steam explosion to produce a fibrous material 401, which is then hydrolyzed and converted, e.g., fermented, to produce the product. The fiber source can be transformed into the fibrous material 401 through a number of possible methods, including at least one shearing process and at least one steam explosion process.
  • For example, one option includes shearing the fiber source, followed by optional screening step(s) and optional additional shearing step(s) to produce a sheared fiber source 402, which can then be steam exploded to produce the fibrous material 401. The steam explosion process is optionally followed by a fiber recovery process to remove liquids or the "liquor" 404, resulting from the steam exploding process. The material resulting from steam exploding the sheared fiber source may be further sheared by optional additional shearing step(s) and/or optional screening step(s).
  • In another method, the fibrous material 401 is first steam exploded to produce a steam exploded fiber source 410. The resulting steam exploded fiber source is then subjected to an optional fiber recovery process to remove liquids, or the liquor. The resulting steam exploded fiber source can then be sheared to produce the fibrous material. The steam exploded fiber source can also be subject to one or more optional screening steps and/or one or more optional additional shearing steps. The process of shearing and steam exploding the fiber source to produce the sheared and steam exploded fibrous material will be further discussed below.
  • The fiber source can be cut into pieces or strips of confetti material prior to shearing or steam explosion. The shearing processes can take place in a dry (e.g., having less than 0.25 percent by weight absorbed water), hydrated, or even while the material is partially or fully submerged in a liquid, such as water or isopropanol. The process can also optimally include steps of drying the output after steam exploding or shearing to allow for additional steps of dry shearing or steam exploding. The steps of shearing, screening, and steam explosion can take place with or without the presence of various chemical solutions.
  • In a steam explosion process, the fiber source or the sheared fiber source is contacted with steam under high pressure, and the steam diffuses into the structures of the fiber source (e.g., the lignocellulosic structures). The steam then condenses under high pressure thereby "wetting" the fiber source. The moisture in the fiber source can hydrolyze any acetyl groups in the fiber source (e.g., the acetyl groups in the hemicellulose fractions), forming organic acids such as acetic and uronic acids. The acids, in turn, can catalyze the depolymerization of hemicellulose, releasing xylan and limited amounts of glucan. The "wet" fiber source (or sheared fiber source, etc.) is then "exploded" when the pressure is released. The condensed moisture instantaneously evaporates due to the sudden decrease in pressure and the expansion of the water vapor exerts a shear force upon the fiber source (or sheared fiber source, etc.). A sufficient shear force will cause the mechanical breakdown of the internal structures (e.g., the the ligocellulosic struructures) of the fiber source.
  • The sheared and steam exploded fibrous material is then converted into a useful product, such as ethanol. In some embodiments, the fibrous material is converted into a fuel. One method of converting the fibrous material into a fuel is by hydrolysis to produce fermentable sugars, 412, which are then fermented to produce the product. Other known and unknown methods of converting fibrous materials into fuels may also be used.
  • In some embodiments, prior to combining the microorganism, the sheared and steam exploded fibrous material 401 is sterilized to kill any competing microorganisms that may be on the fibrous material. For example, the fibrous material can be sterilized by exposing the fibrous material to radiation, such as infrared radiation, ultraviolet radiation, or an ionizing radiation, such as gamma radiation. The microorganisms can also be killed using chemical sterilants, such as bleach (e.g., sodium hypochlorite), chlorhexidine, or ethylene oxide.
  • One method to hydrolyze the sheared and steam exploded fibrous material is by the use of cellulases. Cellulases are a group of enzymes that act synergistically to hydrolyze cellulose. Commercially available Accellerase™ 1000, which contains a complex of enzymes that reduces lignocellulosic biomass into fermentable sugars can also be used.
  • According to current understanding, the components of cellulase include endoglucanases, exoglucanases (cellobiohydrolases), and b-glucosidases (cellobiases). Synergism between the cellulase components exists when hydrolysis by a combination of two or more components exceeds the sum of the activities expressed by the individual components. The generally accepted mechanism of a cellulase system (particularly of T. longibrachiatum) on crystalline cellulose is: endoglucanase hydrolyzes internal β-1,4-glycosidic bonds of the amorphous regions, thereby increasing the number of exposed non-reducing ends. Exoglucanases then cleave off cellobiose units from the nonreducing ends, which in turn are hydrolyzed to individual glucose units by b-gluocosidases. There are several configurations of both endo- and exo- glucanases differing in stereospecificities. In general, the synergistic action of the components in various configurations is required for optimum cellulose hydrolysis. Cellulases, however, are more inclined to hydrolyze the amorphous regions of cellulose. A linear relationship between crystallinity and hydrolysis rates exists whereby higher crystallinity indices correspond to slower enzyme hydrolysis rates. Amorphous regions of cellulose hydrolyze at twice the rate of crystalline regions. The hydrolysis of the sheared and steam exploded fibrous material may be performed by any hydrolyzing biomass process.
  • Steam explosion of biomass sometimes causes the formation of by-products, e.g., toxicants, that are inhibitory to microbial and enzymatic activities. The process of converting the sheared and steam exploded fibrous material into a fuel can therefore optionally include an overliming step prior to fermentation to precipitate some of the toxicants. For example, the pH of the sheared and steam exploded fibrous material may be raised to exceed the pH of 10 by adding calcium hydroxide (Ca(OH)2) followed by a step of lowering the pH to about 5 by adding H2SO4. The overlimed fibrous material may then be used as is without the removal of precipitates. As shown in FIG 23, the optional overliming step occurs just prior to the step of hydrolysis of the sheared and steam exploded fibrous material, but it is also contemplated to perform the overliming step after the hydrolysis step and prior to the fermenting step.
  • FIG. 24 depicts an example of a steam explosion apparatus 460. The steam explosion apparatus 460 includes a reaction chamber 462, in which the fiber source and/or the fibrous material placed through a fiber source inlet 464. The reaction chamber is sealed by closing fiber source inlet valve 465. The reaction chamber further includes a pressurized steam inlet 466 that includes a steam valve 467. The reaction chamber further includes an explosive depressurization outlet 468 that includes an outlet valve 469 in communication with the cyclone 470 through the connecting pipe 472. Once the reaction chamber includes the fiber source and/or sheared fiber source and is sealed by closing valves 465, 467 and 469, steam is delivered into the reaction chamber 462 by opening the steam inlet valve 467 allowing steam to travel through steam inlet 466. Once the reaction chamber reaches target temperature, which can take about 20 - 60 seconds, the holding time begins. The reaction temperature is held at the target temperature for the desired holding time, which typically lasts from about 10 seconds to 5 minutes. At the end of the holding time period, outlet valve is open to allow for explosive depressurization to occur. The process of explosive depressurization propels the contents of the reaction chamber 462 out of the explosive depressurization outlet 468, through the connecting pipe 472, and into the cyclone 470. The steam exploded fiber source or fibrous material then exits the cyclone in a sludge form into the collection bin 474 as much of the remaining steam exits the cyclone into the atmosphere through vent 476. The steam explosion apparatus further includes wash outlet 478 with wash outlet valve 479 in communication with connecting pipe 472. The wash outlet valve 479 is closed during the use of the steam explosion apparatus 460 for steam explosion, but opened during the washing of the reaction chamber 462. The target temperature of the reaction chamber 462 is preferably between 180 and 240 degrees Celsius or between 200 and 220 degrees Celsius. The holding time is preferably between 10 seconds and 30 minutes, or between 30 seconds and 10 minutes, or between 1 minute and 5 minutes.
  • Because the steam explosion process results in a sludge of steam exploded fibrous material, the steam exploded fibrous material may optionally include a fiber recovery process where the "liquor" is separated from the steam exploded fibrous material. This fiber recovery step is helpful in that it enables further shearing and/or screening processes and can allow for the conversion of the fibrous material into fuel. The fiber recovery process occurs through the use of a mesh cloth to separate the fibers from the liquor. Further drying processes can also be included to prepare the fibrous material or steam exploded fiber source for subsequent processing.
  • Any processing technique described herein can be used at pressure above or below normal, earth-bound atmospheric pressure. For example, any process that utilizes radiation, sonication, oxidation, pyrolysis, steam explosion, or combinations of any of these processes to provide materials that include a carbohydrate can be performed under high pressure, which, can increase reaction rates. For example, any process or combination of processes can be performed at a pressure greater than about greater than 25 MPa, e.g., greater than 50 MPa, 75 MPa, 100 MPa, 150 MPa, 200 MPa, 250 MPa, 350 MPa, 500 MPa, 750 MPa, 1,000 MPa, or greater than 1,500 MPa.
  • Combinations of Irradiatting, Sonicating, and Oxidizing Devices
  • In some embodiments, it may be advantageous to combine two or more separate irradiation, sonication, pyrolization, and/or oxidation devices into a single hybrid machine. For such a hybrid machine, multiple processes may be performed in close juxtaposition or even simultaneously, with the benefit of increasing pretreatment throughput and potential cost savings.
  • For example, consider the electron beam irradiation and sonication processes. Each separate process is effective in lowering the mean molecular weight of cellulosic material by an order of magnitude or more, and by several orders of magnitude when performed serially.
  • Both irradiation and sonication processes can be applied using a hybrid electron beam/sonication device as is illustrated in FIG. 25. Hybrid electron beam/sonication device 2500 is pictured above a shallow pool (depth - 3-5 cm) of a slurry of cellulosic material 2550 dispersed in an aqueous, oxidant medium, such as hydrogen peroxide or carbamide peroxide. Hybrid device 2500 has an energy source 2510, which powers both electron beam emitter 2540 and sonication horns 2530..
  • Electron beam emitter 2540 generates electron beams which pass though an electron beam aiming device 2545 to impact the slurry 2550 containing cellulosic material. The electron beam aiming device can be a scanner that sweeps a beam over a range of up to about 6 feet in a direction approximately parallel to the surface of the slurry 2550.
  • On either side of the electron beam emitter 2540 are sonication horns 2530, which deliver ultrasonic wave energy to the slurry 2550. The sonication horns 2530 end in a detachable endpiece 2535 that is in contact with the slurry 2550.
  • The sonication horns 2530 are at risk of damage from long-term residual exposure to the electron beam radiation. Thus, the horns can be protected with a standard shield 2520, e.g., made of lead or a heavy-metal-containing alloy such as Lipowitz metal, which is impervious to electron beam radiation. Precautions must be taken, however, to ensure that the ultrasonic energy is not affected by the presence of the shield. The detachable endpieces 2535, are constructed of the same material and attached to the horns 2530, are used to be in contact with the cellulosic material 2550 and are expected to be damaged. Accordingly, the detachable endpieces 2535 are constructed to be easily replaceable.
  • A further benefit of such a simultaneous electron beam and ultrasound process is that the two processes have complementary results. With electron beam irradiation alone, an insufficient dose may result in cross-linking of some of the polymers in the cellulosic material, which lowers the efficiency of the overall depolymerization process. Lower doses of electron beam irradiation and/or ultrasound radiation may also be used to achieve a similar degree of depolymerization as that achieved using electron beam irradiation and sonication separately.
  • An electron beam device can also be combined with one or more of high-frequency, rotor-stator devices, which can be used as an alternative to ultrasonic energy devices, and performs a similar function.
  • Further combinations of devices are also possible. For example, an ionizing radiation device that produces gamma radiation emitted from, e.g., 60Co pellets, can be combined with an electron beam source and/or an ultrasonic wave source. Shielding requirements may be more stringent in this case.
  • The radiation devices for pretreating biomass discussed above can also be combined with one or more devices that perform one or more pyrolysis processing sequences. Such a combination may again have the advantage of higher throughput. Nevertheless, caution must be observed, as there may be conflicting requirements between some radiation processes and pyrolysis. For example, ultrasonic radiation devices may require the feedstock be immersed in a liquid oxidizing medium. On the other hand, as discussed previously, it may be advantageous for a sample of feedstock undergoing pyrolysis to be of a particular moisture content. In this case, the new systems automatically measure and monitor for a particular moisture content and regulate the same Further, some or all of the above devices, especially the pyrolysis device, can be combined with an oxidation device as discussed previously.
  • PRIMARY PROCESSES Fermentation
  • Generally, various microorganisms can produce a number of useful products, such as a fuel, by operating on, e.g., fermenting the pretreated biomass materials. For example, alcohols, organic acids, hydrocarbons, hydrogen, proteins or mixtures of any of these materials can be produced by fermentation or other processes.
  • The microorganism can be a natural microorganism or an engineered microorganism. For example, the microorganism can be a bacterium, e.g., a cellulolytic bacterium, a fungus, e.g., a yeast, a plant or a protist, e.g., an algae, a protozoa or a fungus-like protist, e.g., a slime mold. When the organisms are compatible, mixtures of organisms can be utilized.
  • To aid in the breakdown of the materials that include the cellulose, one or more enzymes, e.g., a cellulolytic enzyme can be utilized. In some embodiments, the materials that include the cellulose are first treated with the enzyme, e.g., by combining the material and the enzyme in an aqueous solution. This material can then be combined with the microorganism. In other embodiments, the materials that include the cellulose, the one or more enzymes and the microorganism are combined at the concurrently, e.g., by combining in an aqueous solution.
  • Also, to aid in the breakdown of the materials that include the cellulose, the materials can be treated post irradiation with heat, a chemical (e.g., mineral acid, base or a strong oxidizer such as sodium hypochlorite), and/or an enzyme.
  • During the fermentation, sugars released from cellulolytic hydrolysis or the saccharification step, are fermented to, e.g., ethanol, by a fermenting microorganism such as yeast. Suitable fermenting microorganisms have the ability to convert carbohydrates, such as glucose, xylose, arabinose, mannose, galactose, oligosaccharides or polysaccharides into fermentation products. Fermenting microorganisms include strains of the genus Sacchromyces spp. e.g., Sacchromyces cerevisiae (baker's yeast), Saccharomyces distaticus, Saccharomyces uvarum; the genus Kluyveromyces, e.g., species Kluyveromyces marxianus, Kluyveromyces fragilis; the genus Candida, e.g., Candida pseudotropicalis, and Candida brassicae, the genus Clavispora, e.g., species Clavispora lusitaniae and Clavispora opuntiae the genus Pachysolen, e.g., species Pachysolen tannophilus, the genus Bretannomyces, e.g., species Bretannomyces clausenii (Philippidis, G. P.,1996, Cellulose bioconversion technology, in Handbook on Bioethanol: Production and Utilization, Wyman, C.E., ed., Taylor & Francis, Washington, DC, 179-212).
  • Commercially available yeast include, for example, Red Star®/Lesaffre Ethanol Red (available from Red Star/Lesaffre, USA) FALI® (available from Fleischmann's Yeast, a division of Bums Philip Food Inc., USA), SUPERSTART® (available from Alltech), GERT STRAND® (available from Gert Strand AB, Sweden) and FERMOL® (available from DSM Specialties).
  • Bacteria that can ferment bimoss to ethanol and other products include, e.g., Zymomonas mobilis and Clostridium thermocellum (Philippidis, 1996, supra). Leschine et al. (International Journal of Systematic and Evolutionary Mlcrobiology 2002, 52,1155-1160) isolated an anaerobic, mesophilic, cellulolytic bacterium from forest soil, Clostridium phytofermentans sp. nov., which converts cellulose to ethanol.
  • Fermentation of biomass to ethanol and other products may be carried out using certain types of thermophilic or genetically engineered microorganisms, such Thermoanaerobacter species, including T. mathranii, and yeast species such as Pichia species. An example of a strain of T. mathranii is A3M4 described in Sonne-Hansen et al. (Applied Microbiology and Biotechnology 1993, 38, 537-541) or Ahring et al. (Arch. Microbiol. 1997, 168, 114-119).
  • Yeast and Zymomonas bacteria can be used for fermentation or conversion. The optimum pH for yeast is from about pH 4 to 5, while the optimum pH for Zymomonas is from about pH 5 to 6. Typical fermentation times are about 24 to 96 hours with temperatures in the range of 26 °C to 40 °C, however thermophilic microorganisms prefer higher temperatures.
  • Enzymes which break down biomass, such as cellulose, to lower molecular weight carbohydrate-containing materials, such as glucose, during saccharification are referred to as cellulolytic enzymes or cellulase. These enzymes may be a complex of enzymes that act synergistically to degrade crystalline cellulose. Examples of cellulolytic enzymes include: endoglucanases, cellobiohydrolases, and cellobiases (β-glucosidases). A cellulosic substrate is initially hydrolyzed by endoglucanases at random locations producing oligomeric intermediates. These intermediates are then substrates for exo-splitting glucanases such as cellobiohydrolase to produce cellobiose from the ends of the cellulose polymer. Cellobiose is a water-soluble β-1,4-linked dimer of glucose. Finally cellobiase cleaves cellobiose to yield glucose.
  • A cellulase is capable of degrading biomass and may be of fungal or bacterial origin. Suitable enzymes include cellulases from the genera Bacillus, Pseudomonas, Humicola, Fusarium, Thielavia, Acremonium, Chrysosporium and Trichoderma, and include species of Humicola, Coprinus, Thielavia, Fusarium, Myceliophthora, Acremonium, Cephalosporium, Scytalidium, Penicillium or Aspergillus (see, e.g., EP 458162 ), especially those produced by a strain selected from the species Humicola insolens (reclassified as Scytalidium thermophilum, see, e.g., U.S. Patent No. 4,435,307 ), Coprinus cinereus, Fusarium oxysporum, Myceliophthora thermophila, Meripilus giganteus, Thielavia terrestris, Acremonium sp., Acremonium persicinum, Acremonium acremonium, Acremonium brachypenium, Acremonium dichromosporum, Acremonium obclavatum, Acremonium pinkertoniae, Acremonium roseogriseum, Acremonium incoloratum, and Acremonium furatum; preferably from the species Humicola insolens DSM 1800, Fusarium axysporum DSM 2672, Myceliophthora thermophila CBS 117.65, Cephalosporium sp. RYM-202, Acremonium sp. CBS 478.94, Acremonium sp. CBS 265.95, Acremonium persicinum CBS 169.65, Acremonium acremonium AHU 9519, Cephalosporium sp. CBS 535.71, Acremonium brachypenium CBS 866.73, Acremonium dichromosporum CBS 683.73, Acremonium obclavatum CBS 311.74, Acremonium pinkertoniae CBS 157.70, Acremonium raseogriseum CBS 134.56, Acremonium incoloratum CBS 146.62, and Acremonium furatum CBS 299.70H. Cellulolytic enzymes may also be obtained from Chrysosporium, preferably a strain of Chrysosporium lucknowense. Additionally, Trichoderma (particularly Trichoderma viride, Trichoderma reesei, and Trichoderma koningii), alkalophilic Bacillus (see, for example, U.S. Patent No. 3,844,890 and EP 458162 ), and Streptomyces (see, e.g., EP 458162 ) may be used.
  • Anaerobic cellulolytic bacteria have also been isolated from soil, e.g., a novel cellulolytic species of Clostiridium, Clostridium phytofermentans sp. nov. (see Leschine et. al, International Journal of Systematic and Evolutionary Microbiology (2002), 52, 1155-1160).
  • Cellulolytic enzymes using recombinant technology can also be used (see, e.g., WO 2007/071818 and WO 2006/110891 ).
  • The cellulolytic enzymes used can be produced by fermentation of the above-noted microbial strains on a nutrient medium containing suitable carbon and nitrogen sources and inorganic salts, using procedures known in the art (see, e.g., Bennett, J.W. and LaSure, L. (eds.), More Gene Manipulations in Fungi, Academic Press, CA 1991). Suitable media are available from commercial suppliers or may be prepared according to published compositions (e.g., in catalogues of the American Type Culture Collection). Temperature ranges and other conditions suitable for growth and cellulase production are known in the art (see, e.g., Bailey, J.E., and Ollis, D.F., Biochemical Engineering Fundamentals, McGraw-Hill Book Company, NY,1986).
  • Treatment of cellulose with cellulase is usually carried out at temperatures between 30 °C and 65°C. Cellulases are active over a range of pH of about 3 to 7. A saccharification step may last up to 120 hours. The cellulase enzyme dosage achieves a sufficiently high level of cellulose conversion. For example, an appropriate cellulase dosage is typically between 5.0 and 50 Filter Paper Units (FPU or IU) per gram of cellulose. The FPU is a standard measurement and is defined and measured according to Ghose (1987, Pure and Appl. Chem. 59:257-268).
  • Gasification
  • In addition to using pyrolysis for pre-treatment of feedstock, pyrolysis can also be used to process pre-treated feedstock to extract useful materials. In particular, a form of pyrolysis known as gasification can be employed to generate fuel gases along with various other gaseous, liquid, and solid products. To perform gasification, the pre-treated feedstock is introduced into a pyrolysis chamber and heated to a high temperature, typically 700 °C or more. The temperature used depends upon a number of factors, including the nature of the feedstock and the desired products.
  • Quantities of oxygen (e.g., as pure oxygen gas and/or as air) and steam (e.g., superheated steam) are also added to the pyrolysis chamber to facilitate gasification. These compounds react with carbon-containing feedstock material in a multiple-step reaction to generate a gas mixture called synthesis gas (or "syngas"). Essentially, during gasification, a limited amount of oxygen is introduced into the pyrolysis chamber to allow some feedstock material to combust to form carbon monoxide and generate process heat. The process heat can then be used to promote a second reaction that converts additional feedstock material to hydrogen and carbon monoxide.
  • In a first step of the overall reaction, heating the feedstock material produces a char that can include a wide variety of different hydrocarbon-based species. Certain volatile materials can be produced (e.g., certain gaseous hydrocarbon materials), resulting in a reduction of the overall weight of the feedstock material. Then, in a second step of the reaction, some of the volatile material that is produced in the first step reacts with oxygen in a combustion reaction to produce both carbon monoxide and carbon dioxide. The combustion reaction releases heat, which promotes the third step of the reaction. In the third step, carbon dioxide and steam (e.g., water) react with the char generated in the first step to form carbon monoxide and hydrogen gas. Carbon monoxide can also react with steam, in a water gas shift reaction, to form carbon dioxide and further hydrogen gas.
  • Gasification can be used as a primary process to generate products directly from pretreated feedstock for subsequent transport and/or sale, for example. Alternatively, or in addition, gasification can be used as an auxiliary process for generating fuel for an overall processing system. The hydrogen-rich syngas that is generated via the gasification process can be burned, for example, to generate electricity and/or process heat that can be directed for use at other locations in the processing system. As a result, the overall processing system can be at least partially self-sustaining. A number of other products, including pyrolysis oils and gaseous hydrocarbon-based substances, can also be obtained during and/or following gasification; these can be separated and stored or transported as desired.
  • A variety of different pyrolysis chambers are suitable for gasification of pro-treated feedstock, including the pyrolysis chambers disclosed herein. In particular, fluidized bed reactor systems, in which the pre-treated feedstock is fluidized in steam and oxygen/air, provide relatively high throughput and straightforward recovery of products. Solid char that remains following gasification in a fluidized bed system (or in other pyrolysis chambers) can be burned to generate additional process heat to promote subsequent gasification reactions.
  • POST-PROCESSING Distillation
  • After fermentation, the resulting fluids can be distilled using, for example, a "beer column" to separate ethanol and other alcohols from the majority of water and residual solids. The vapor exiting the beer column can be 35% by weight ethanol and fed to a rectification column. A mixture of nearly azeotropic (92.5%) ethanol and water from the rectification column can be purified to pure (99.5%) ethanol using vapor-phase molecular sieves. The beer column bottoms can be sent to the first effect of a three-effect evaporator. The rectification column reflux condenser can provide heat for this first effect. After the first effect, solids can be separated using a centrifuge and dried in a rotary dryer. A portion (25%) of the centrifuge effluent can be recycled to fermentation and the rest sent to the second and third evaporator effects. Most of the evaporator condensate can be returned to the process as fairly clean condensate with a small portion split off to waste water treatment to prevent build-up of low-boiling compounds.
  • Waste water treatment
  • Wastewater treatment is used to minimize makeup water requirements of the plant by treating process water for reuse within the plant. Wastewater treatment can also produce fuel (e.g., sludge and biogas) that can be used to improve the overall efficiency of the ethanol production process. For example, as described in further detail below, sludge and biogas can be used to create steam and electricity that can be used in various plant processes.
  • Wastewater is initially pumped through a screen (e.g., a bar screen) to remove large particles, which are collected in a hopper. In some embodiments, the large particles are sent to a landfill. Additionally or alternatively, the large particles are burned to create steam and/or electricity as described in further detail below. In general, the spacing on the bar screen is between 1/4 inch to 1 inch spacing (e.g.,1/2 inch spacing).
  • The wastewater then flows to an equalization tank, where the organic concentration of the wastewater is equalized during a retention time. In general, the retention time is between 8 hours and 36 hours (e.g., 24 hours). A mixer is disposed within the tank to stir the contents of the tank. In some embodiments, a plurality of mixers disposed throughout the tank are used to stir the contents of the tank. In certain embodiments, the mixer substantially mixes the contents of the equalization tank such that conditions (e.g., wastewater concentration and temperature) throughout the tank are uniform.
  • A first pump moves water from the equalization tank through a liquid-to-liquid heat exchanger. The heat exchanger is controlled (e.g., by controlling the flow rate of fluid through the heat exchanger) such that wastewater exiting the heat exchanger is at a desired temperature for anaerobic treatment. For example, the desired temperature for anaerobic treatment can be between 40 °C to 60 °C.
  • After exiting the heat exchanger, the wastewater enters one or more anaerobic reactors. In some embodiments, the concentration of sludge in each anaerobic reactor is the same as the overall concentration of sludge in the wastewater. In other embodiments, the anaerobic reactor has a higher concentration of sludge than the overall concentration of sludge in the wastewater.
  • A nutrient solution containing nitrogen and phosphorus is metered into each anaerobic reactor containing wastewater. The nutrient solution reacts with the sludge in the anaerobic reactor to produce biogas which can contain 50% methane and have a heating value of approximately 12,000 British thermal units, or Btu, per pound). The biogas exits each anaerobic reactor through a vent and flows into a manifold, where a plurality of biogas streams are combined into a single stream. A compressor moves the stream of biogas to a boiler or a combustion engine as described in further detail below. In some embodiments, the compressor also moves the single stream of biogas through a desulphurization catalyst. Additionally or alternatively, the compressor can move the single stream of biogas through a sediment trap.
  • A second pump moves anaerobic effluent from the anaerobic reactors to one or more aerobic reactors (e.g., activated sludge reactors). An aerator is disposed within each aerobic reactor to mix the anaerobic effluent, sludge, oxygen (e.g., oxygen contained in air). Within each aerobic reactor, oxidation of cellular material in the anaerobic effluent produces carbon dioxide, water, and ammonia.
  • Aerobic effluent moves (e.g., via gravity) to a separator, where sludge is separated from treated water. Some of the sludge is returned to the one or more aerobic reactors to create an elevated sludge concentration in the aerobic reactors, thereby facilitating the aerobic breakdown of cellular material in the wastewater. A conveyor removes excess sludge from the separator. As described in further detail below, the excess sludge is used as fuel to create steam and/or electricity.
  • The treated water is pumped from the separator to a settling tank. Solids dispersed throughout the treated water settle to the bottom of the settling tank and are subsequently removed. After a settling period, treated water is pumped from the settling tank through a fine filter to remove any additional solids remaining in the water. In some embodiments, chlorine is added to the treated water to kill pathogenic bacteria. In some embodiments, one or more physical-chemical separation techniques are used to further purify the treated water. For example, treated water can be pumped through a carbon adsorption reactor. As another example, treated water can pumped through a reverse osmosis reactor.
  • Waste combustion
  • The production of alcohol from biomass can result in the production of various by-product streams useful for generating steam and electricity to be used in other parts of the plant. For example, steam generated from burning by-product streams can be used in the distillation process. As another example, electricity generated from burning by-product streams can be used to power electron beam generators and ultrasonic transducers used in pretreatment.
  • The by-products used to generate steam and electricity are derived from a number of sources throughout the process. For example, anaerobic digestion of wastewater produces a biogas high in methane and a small amount of waste biomass (sludge). As another example, post-distillate solids (e.g., unconverted lignin, cellulose, and hemicellulose remaining from the pretreatment and primary processes) can be used as a fuel.
  • The biogas is diverted to a combustion engine connected to an electric generator to produce electricity. For example, the biogas can be used as a fuel source for a spark-ignited natural gas engine. As another example, the biogas can be used as a fuel source for a direct-injection natural gas engine. As another example, the biogas can be used as a fuel source for a combustion turbine. Additionally or alternatively, the combustion engine can be configured in a cogeneration configuration. For example, waste heat from the combustion engines can be used to provide hot water or steam throughout the plant.
  • The sludge, and post-distillate solids are burned to heat water flowing through a heat exchanger. In some embodiments, the water flowing through the heat exchanger is evaporated and superheated to steam. In certain embodiments, the steam is used in the pretreatment rector and in heat exchange in the distillation and evaporation processes. Additionally or alternatively, the steam expands to power a multi-stage steam turbine connected to an electric generator. Steam exiting the steam turbine is condensed with cooling water and returned to the heat exchanger for reheating to steam. In some embodiments, the flow rate of water through the heat exchanger is controlled to obtain a target electricity output from the steam turbine connected to an electric generator. For example, water can be added to the heat exchanger to ensure that the steam turbine is operating above a threshold condition (e.g., the turbine is spinning fast enough to turn the electric generator).
  • While certain embodiments have been described, other embodiments are possible.
  • As an example, while the biogas is described as being diverted to a combustion engine connected to an electric generator, in certain embodiments, the biogas can be passed through a fuel reformer to produce hydrogen. The hydrogen is then converted to electricity through a fuel cell.
  • As another example, while the biogas is described as being burned apart from the sludge and post-distillate solids, in certain embodiments, all of the waste by-products can be burned together to produce steam.
  • PRODUCTS / CO-PRODUCTS Alcohols
  • The alcohol produced can be a monohydroxy alcohol, e.g., ethanol, or a polyhydroxy alcohol, e.g., ethylene glycol or glycerin. Examples of alcohols that can be produced include methanol, ethanol, propanol, isopropanol, butanol, e.g., n-, sec- or t-butanol, ethylene glycol, propylene glycol, 1, 4-butane diol, glycerin or mixtures of these alcohols.
  • Each of the alcohols produced by the plant have commercial value as industrial feedstock. For example, ethanol can be used in the manufacture of varnishes and perfume. As another example, methanol can be used as a solvent used as a component in windshield wiper fluid. As still another example, butanol can be used in plasficizers, resins, lacquers, and brake fluids.
  • Bioethanol produced by the plant is valuable as an ingredient used in the food and beverage industry. For example, the ethanol produced by the plant can be purified to food grade alcohol and used as a primary ingredient in the alcoholic beverages.
  • Bioethanol produced by the plant also has commercial value as a transportation fuel. The use of ethanol as a transportation fuel can be implemented with relatively little capital investment from spark ignition engine manufacturers and owners (e.g., changes to injection timing, fuel-to-air ratio, and components of the fuel injection system). Many automotive manufacturers currently offer flex-fuel vehicles capable of operation on ethanol/gasoline blends up to 85% ethanol by volume (e.g., standard equipment on a Chevy Tahoe 4 x 4).
  • Bioethanol produced by this plant can be used as an engine fuel to improve environmental and economic conditions beyond the location of the plant. For example, ethanol produced by this plant and used as a fuel can reduce greenhouse gas emissions from manmade sources (e.g., transportation sources). As another example, ethanol produced by this plant and used as an engine fuel can also displace consumption of gasoline refined from oil.
  • Bioethanol has a greater octane number than conventional gasoline and, thus, can be used to improve the performance (e.g., allow for higher compression ratios) of spark ignition engines. For example, small amounts (e.g.,10% by volume) of ethanol can be blended with gasoline to act as an octane enhancer for fuels used in spark ignition engines. As another example, larger amounts (e.g., 85% by volume) of ethanol can be blended with gasoline to further increase the fuel octane number and displace larger volumes of gasoline.
  • Bioethanol strategies are discussed, e.g., by DiPardo in Journal of Outlook for Biomass Ethanol Production and Demand (EIA Forecasts), 2002; Sheehan in Biotechnology Progress, 15:8179,1999; Martin in Enzyme Microbes Technology, 31:274, 2002; Greer in BioCycle, 61-65, April 2005; Lynd in Microbiology and Molecular Biology Reviews, 66:3, 506-577, 2002; Ljungdahl et al. in U.S. Patent No. 4,292,406 ; and Bellamy in U.S. Patent No. 4,094,742 .
  • Organic acids
  • The organic acids produced can include monocarboxylic acids or a polycarboxylic acids. Examples of organic acids include formic acid, acetic acid, propionic acid, butyric acid, valeric acid, caproic, palmitic acid, stearic acid, oxalic acid, malonic acid, succinic acid, glutaric acid, oleic acid, linoleic acid, glycolic acid, lactic acid, γ-hydroxybutyric acid or mixtures of these acids.
  • Foodstocks
  • In some embodiments, all or a portion of the fermentation process can be interrupted before the cellulosic material is completely converted to ethanol. The intermediate fermentation products include high concentrations of sugar and carbohydrates. These intermediate fermentation products can be used in preparation of food for human or animal consumption. In some embodiments, irradiation pretreatment of the cellulosic material will render the intermediate fermentation products sterile (e.g., fit for human consumption). In some embodiments, the intermediate fermentation products will require post-processing prior to use as food. For example, a dryer can be used to remove moisture from the intermediate fermentation products to facilitate storage, handling, and shelf-life. Additionally or alternatively, the intermediate fermentation products can be ground to a fine particle size in a stainless-steel laboratory mill to produce a flour-like substance.
  • Animal feed
  • Distillers grains and solubles can be converted into a valuable byproduct of the distillation-dehydration process. After the distillation-dehydration process, distillers grains and solubles can be dried to improve the ability to store and handle the material. The resulting dried distillers grains and solubles (DDGS) is low in starch, high in fat, high in protein, high in fiber, and high in phosphorous. Thus, for example, DDGS can be valuable as a source of animal feed (e.g., as a feed source for dairy cattle). DDGS can be subsequently combined with nutritional additives to meet specific dietary requirements of specific categories of animals (e.g., balancing digestible lysine and phosphorus for swine diets).
  • Pharmaceuticals
  • The pretreatment processes discussed above can be applied to plants with medicinal properties. In some embodiments, sonication can stimulate bioactivity and/or bioavailabilty of the medicinal components of plants with medicinal properties. Additionally or alternatively, irradiation stimulates bioactivity and/or bioavailabilty of the medicinal components of plants with medicinal properties. For example, sonication and irradiation can be combined in the pretreatment of willow bark to stimulate the production of salicin.
  • Nutriceuticals
  • In some embodiments, intermediate fermentation products (e.g., products that include high concentrations of sugar and carbohydrates) can be supplemented to create a nutriceutical. For example, intermediate fermentation products can be supplemented with calcium create a nutriceutical that provides energy and helps improve or maintain bone strength.
  • Co-Products Lignin Residue
  • As described above, lignin containing residues from primary and pretreatment processes has value as a high/medium energy fuel and can be used to generate power and steam for use in plant processes. However, such lignin residues are a new type of solids fuel and there is little demand for it outside of the plant boundaries, and the costs of drying it for transportation only subtract from its potential value. In some cases, gasification of the lignin residues can converting it to a higher-value product with lower cost.
  • Other Co-Products
  • Cell matter, furfural, and acetic acid have been identified as potential co-products of biomass-to-fuel processing facilities. Interstitial cell matter could be valuable, but might require significant purification. Markets for furfural and acetic acid are in place, although it is unlikely that they are large enough to consume the output of a fully commercialized lignocellulose-to-ethanol industry.
  • EXAMPLES
  • The following Examples are intended to illustrate, and do not limit the teachings of this disclosure.
  • Example 1 - Preparation Of Fibrous Material From Polycoated Paper
  • A 1500 pound skid of virgin, half-gallon juice cartons made of un-printed polycoated white Kraft board having a bulk density of 20 lb/ft3 was obtained from International Paper. Each carton was folded flat, and then fed into a 3 hp Flinch Baugh shredder at a rate of approximately 15 to 20 pounds per hour. The shredder was equipped with two 12 inch rotary blades, two fixed blades and a 0.30 inch discharge screen. The gap between the rotary and fixed blades was adjusted to 0.10 inch. The output from the shredder resembled confetti having a width of between 0.1 inch and 0.5 inch, a length of between 0.25 inch and 1 inch and a thickness equivalent to that of the starting material (about 0.075 inch).
  • The confetti-like material was fed to a Munson rotary knife cutter, Model SC30. Model SC30 is equipped with four rotary blades, four fixed blades, and a discharge screen having 1/8 inch openings. The gap between the rotary and fixed blades was set to approximately 0.020 inch. The rotary knife cutter sheared the confetti-like pieces across the knife-edges, tearing the pieces apart and releasing a fibrous material at a rate of about one pound per hour. The fibrous material had a BET surface area of 0.9748 m2/g +/- 0.0167 m2/g, a porosity of 89.0437 percent and a bulk density (@0.53 psia) of 0.1260 g/mL. An average length of the fibers was 1.141 mm and an average width of the fibers was 0.027 mm, giving an average L/D of 42:1. A scanning electron micrograph of the fibrous material is shown in FIG. 26 at 25 X magnification.
  • Example 2 - Preparation Of Fibrous Material From Bleached Kraft Board
  • A 1500 pound skid of virgin bleached white Kraft board having a bulk density of 30 lb/ft3 was obtained from International Paper. The material was folded flat, and then fed into a 3 hp Flinch Baugh shredder at a rate of approximately 15 to 20 pounds per hour. The shredder was equipped with two 12 inch rotary blades, two fixed blades and a 0.30 inch discharge screen. The gap between the rotary and fixed blades was adjusted to 0.10 inch. The output from the shredder resembled confetti having a width of between 0.1 inch and 0.5 inch, a length of between 0.25 inch and 1 inch and a thickness equivalent to that of the starting material (about 0.075 inch). The confetti-like material was fed to a Munson rotary knife cutter, Model SC30. The discharge screen had 1/8 inch openings. The gap between the rotary and fixed blades was set to approximately 0.020 inch. The rotary knife cutter sheared the confetti-like pieces, releasing a fibrous material at a rate of about one pound per hour. The fibrous material had a BET surface area of 1.1316 m2/g +/- 0.0103 m2/g, a porosity of 88.3285 percent and a bulk density (@0.53 psia) of 0.1497 g/mL. An average length of the fibers was 1.063 mm and an average width of the fibers was 0.0245 mm, giving an average L/D of 43:1. A scanning electron micrographs of the fibrous material is shown in FIG 27 at 25 X magnification.
  • Example 3 - Preparation Of Twice Sheared Fibrous Material From Bleached Kraft Board
  • A 1500 pound skid of virgin bleached white Kraft board having a bulk density of 30 lb/ft3 was obtained from International Paper. The material was folded flat, and then fed into a 3 hp Flinch Baugh shredder at a rate of approximately 15 to 20 pounds per hour. The shredder was equipped with two 12 inch rotary blades, two fixed blades and a 0.30 inch discharge screen. The gap between the rotary and fixed blades was adjusted to 0.10 inch. The output from the shredder resembled confetti (as above). The confetti-like material was fed to a Munson rotary knife cutter, Model SC30. The discharge screen had 1/16 inch openings. The gap between the rotary and fixed blades was set to approximately 0.020 inch. The rotary knife cutter the confetti-like pieces, releasing a fibrous material at a rate of about one pound per hour. The material resulting from the first shearing was fed back into the same setup described above and sheared again. The resulting fibrous material had a BET surface area of 1.4408 m2/g +/-0.0156 m2/g, a porosity of 90.8998 percent and a bulk density (@0.53 psia) of 0.1298 g/mL. An average length of the fibers was 0.891 mm and an average width of the fibers was 0.026 mm, giving an average L/D of 34:1. A scanning electron micrograph of the fibrous material is shown in FIG 28 at 25 X magnification.
  • Example 4 - Preparation Of Thrice Sheared Fibrous Material From Bleached Kraft Board
  • A 1500 pound skid of virgin bleached white Kraft board having a bulk density of 30 lb/ft3 was obtained from International Paper. The material was folded flat, and then fed into a 3 hp Flinch Baugh shredder at a rate of approximately 15 to 20 pounds per hour. The shredder was equipped with two 12 inch rotary blades, two fixed blades and a 0.30 inch discharge screen. The gap between the rotary and fixed blades was adjusted to 0.10 inch. The output from the shredder resembled confetti (as above). The confetti-like material was fed to a Munson rotary knife cutter, Model SC30. The discharge screen had 1/8 inch openings. The gap between the rotary and fixed blades was set to approximately 0.020 inch. The rotary knife cutter sheared the confetti-like pieces across the knife-edges. The material resulting from the first shearing was fed back into the same setup and the screen was replaced with a 1/16 inch screen. This material was sheared. The material resulting from the second shearing was fed back into the same setup and the screen was replaced with a 1/32 inch screen. This material was sheared. The resulting fibrous material had a BET surface area of 1.6897 m2/g +/- 0.0155 m2/g, a porosity of 87.7163 percent and a bulk density (@0.53 psia) of 0.1448 g/mL. An average length of the fibers was 0.824 mm and an average width of the fibers was 0.0262 mm, giving an average L/D of 32:1. A scanning electron micrograph of the fibrous material is shown in FIG 29 at 25 X magnification.
  • Example 5 - Preparation Of Densified Fibrous Material From Bleached Kraft Board Without Added Binder
  • Fibrous material was prepared according to Example 2. Approximately 1 lb of water was sprayed onto each 10 lb of fibrous material. The fibrous material was densified using a California Pellet Mill 1100 operating at 75 °C. Pellets were obtained having a bulk density ranging from about 7 lb/ft3 to about 15 lb/ft3.
  • Example 6 - Preparation Of Densified Fibrous Material From Bleached Kraft Board With Binder
  • Fibrous material was prepared according to Example 2.
  • A 2 weight percent stock solution of POLYOX WSR N10 (polyethylene oxide) was prepared in water.
  • Approximately 1 lb of the stock solution was sprayed onto each 10 lb of fibrous material. The fibrous material was densified using a California Pellet Mill 1100 operating at 75 °C. Pellets were obtained having a bulk density ranging from about 15 lb/ft3 to about 40 lb/ft3.
  • Example 7 - Reducing the Molecular Weight of Cellulose in Fibrous Kraft Paper by Gamma Radiation with Minimum Oxidation
  • Fibrous material is prepared according to Example 4. The fibrous Kraft paper is densified according to Example 5.
  • The densified pellets are placed in a glass ampoule having a maximum capacity of 250 mL. The glass ampoule is evacuated under high vacuum (10-5 torr) for 30 minutes, and then back-filled with argon gas. The ampoule is sealed under argon. The pellets in the ampoule are irradiated with gamma radiation for about 3 hours at a dose rate of about 1 Mrad per hour to provide an irradiated material in which the cellulose has a lower molecular weight than the fibrous Kraft starting material.
  • Example 8 - Reducing the Molecular Weight of Cellulose in Fibrous Kraft Paper by Gamma Radiation with Maximum Oxidation
  • Fibrous material is prepared according to Example 4. The fibrous Kraft paper is densified according to Example 5.
  • The densified pellets are placed in a glass ampoule having a maximum capacity of 250 mL. The glass ampoule is sealed under an atmosphere of air. The pellets in the ampoule are irradiated with gamma radiation for about 3 hours at a dose rate of about 1 Mrad per hour to provide an irradiated material in which the cellulose has a lower molecular weight than the fibrous Kraft starting material.
  • Example 9 - Methods of Determining Molecular Weight of Cellulosic and Lignocellulosic Materials by Gel Permeation Chromatography
  • Cellulosic and lignocellulosic materials for analysis were treated according to Example 4. Sample materials presented in the following tables include Kraft paper (P), wheat straw (WS), alfalfa (A), and switchgrass (SG). The number "132" of the Sample ID refers to the particle size of the material after shearing through a 1/32 inch screen. The number after the dash refers to the dosage of radiation (MRad) and "US" refers to ultrasonic treatment. For example, a sample ID "P132-10" refers to Kraft paper that has been sheared to a particle size of 132 mesh and has been irradiated with 10 MRad. Table 1. Peak Average Molecular Weight of Irradiated Kraft Paper
    Sample Source Sample ID Dosage1 (Mrad) Ultrasound2 Average MW± Std Dev.
    Kraft Paper P132 0 No 32853±10006
    P132-10 10 " 61398 ± 2468**
    P132-100 100 " 8444 ± 580
    P132-181 181 " 6668 ± 77
    P132-US 0 Yes 3095 ± 1013
    **Low doses of radiation appear to increase the molecular weight of some materials
    1Dosage Rate = 1MRad/hour
    2Treatment for 30 minutes with 20kHz ultrasound using a 1000W horn under re-circulating conditions with the material dispersed in water.
    Table 2. Peak Average Molecular Weight of Irradiated Materials
    Sample ID Peak # Dosage1 (MRad) Ultrasound2 Average MW ± Std Dev.
    WS132 1 0 No " 1407411 ± 175191
    2 " 39145 ± 3425
    3 " " 2886 ± 177
    WS132-10* 1 10 " 26040 ± 3240
    WS132-100* 1 100 " 23620 ± 453
    A132 1 0 " 1604886 ± 151701
    2 " " 37525 ± 3751
    3 " " 2853 ± 490
    A132-10* 1 10 " 50853 ± 1665
    2 " " 2461 ± 17
    A132-100* 1 100 " 38291 ± 2235
    2 " " 2487 ± 15
    SG132 1 0 " 1557360 ± 83693
    2 " " 42594 ± 4414
    3 " " 3268 ± 249
    SG132-10* 1 10 " 60888 ± 9131
    SG132-100* 1 100 " 22345 ± 3797
    SG132-10-US 1 10 Yes 86086 ± 43518
    2 " " 2247 ± 468
    SG132-100-US 1 100 " 4696 ± 1465
    *Peaks coalesce after treatment
    **Low doses of radiation appear to increase the molecular weight of some materials
    1Dosage Rate = 1MRad/hour
    2Treatment for 30 minutes with 20kHz ultrasound using a 1000W horn under re-circulating conditions with the material dispersed in water.
  • Gel Permeation Chromatography (GPC) is used to determine the molecular weight distribution of polymers. During GPC analysis, a solution of the polymer sample is passed through a column packed with a porous gel trapping small molecules. The sample is separated based on molecular size with larger molecules eluting sooner than smaller molecules. The retention time of each component is most often detected by refractive index (RI), evaporative light scattering (ELS), or ultraviolet (UV) and compared to a calibration curve. The resulting data is then used to calculate the molecular weight distribution for the sample.
  • A distribution of molecular weights rather than a unique molecular weight is used to characterize synthetic polymers. To characterize this distribution, statistical averages are utilized. The most common of these averages are the "number average molecular weight" (Mn) and the "weight average molecular weight" (Mw).
  • Mn is similar to the standard arithmetic mean associated with a group of numbers. When applied to polymers, Mn refers to the average molecular weight of the molecules in the polymer. Mn is calculated affording the same amount of significance to each molecule regardless of its individual molecular weight. The average Mn is calculated by the following formula where Ni is the number of molecules with a molar mass equal to Mi. M n = i N i M i i N i
    Figure imgb0004
  • Mw is another statistical descriptor of the molecular weight distribution that places a greater emphasis on larger molecules than smaller molecules in the distribution. The formula below shows the statistical calculation of the weight average molecular weight. M w = i N i M i 2 i N i M i
    Figure imgb0005
  • The polydispersity index or PI is defined as the ratio of Mw/Mn. The larger the PI, the broader or more disperse the distribution. The lowest value that a PI can be is 1. This represents a monodisperse sample; that is, a polymer with all of the molecules in the distribution being the same molecular weight.
  • The peak molecular weight value (Mp) is another descriptor defined as the mode of the molecular weight distribution. It signifies the molecular weight that is most abundant in the distribution. This value also gives insight to the molecular weight distribution.
  • Most GPC measurements are made relative to a different polymer standard. The accuracy of the results depends on how closely the characteristics of the polymer being analyzed match those of the standard used. The expected error in reproducibility between different series of determinations, calibrated separately, is ca. 5-10% and is characteristic to the limited precision of GPC determinations. Therefore, GPC results are most useful when a comparison between the molecular weight distribution of different samples is made during the same series of determinations.
  • The lignocellulosic samples required sample preparation prior to GPC analysis. First, a saturated solution (8.4% by weight) of lithium chloride (LiCl) was prepared in dimethyl acetamide (DMAc). Approximately 100 mg of the sample was added to approximately 10 g of a freshly prepared saturated LiCl/DMAc solution, and the mixture was heated to approximately 150°C-170°C with stirring for 1 hour. The resulting solutions were generally light- to dark-yellow in color. The temperature of the solutions were decreased to approximately 100°C and heated for an additional 2 hours. The temperature of the solutions were then decreased to approximately 50°C and the sample solution was heated for approximately 48 to 60 hours. Of note, samples irradiated at 100 MRad were more easily solubilized as compared to their untreated counterpart. Additionally, the sheared samples (denoted by the number 132) had slightly lower average molecular weights as compared with uncut samples.
  • The resulting sample solutions were diluted 1:1 using DMAc as solvent and were filtered through a 0.45 µm PTFE filter. The filtered sample solutions were then analyzed by GPC. The peak average molecular weight (Mp) of the samples, as determined by Gel Permeation Chromatography (GPC), are summarized in Tables 1 and 2.Each sample was prepared in duplicate and each preparation of the sample was analyzed in duplicate (two injections) for a total of four injections per sample. The EasiCal polystyrene standards PS1A and PS1B were used to generate a calibration curve for the molecular weight scale from about 580 to 7,500,00 Daltons. Table 3. GPC Analysis Conditions
    Instrument: Waters Alliance GPC 2000
    Plgel 10µ Mixed-B
    Columns (3): S/N's: 10M-MB-148-83; 10M-MB-148-84; 10M-MB-174-129
    Mobile Phase (solvent): 0.5% LiCl in DMAc (1.0 mL/min.)
    Column/Detector Temperature: 70 °C
    Injector Temperature: 70 °C
    Sample Loop Size: 323.5 µL
  • Example 10- Determing Cyrstallinity of Irradiated Material by X-Ray Diffraction
  • X-ray diffraction (XRD) is a method by which a crystalline sample is irradiated with monoenergetic x-rays. The interaction of the lattice structure of the sample with these x-rays is recorded and provides information about the crystalline structure being irradiated. The resulting characteristic "fingerprint" allows for the identification of the crystalline compounds present in the sample. Using a whole-pattern fitting analysis (the Rietvelt Refinement), it is possible to perform quantitative analyses on samples containing more than one crystalline compound. Table 4. XRD Data including Domain Size and % Crystallinity
    Sample ID Domain Size (Å) % Crystallinity
    P132 55 55
    P132-10 46 58
    P132-100 50 55
    P132-181 48 52
    P132-US 26 40
    A132 28 42
    A132-10 26 40
    A132-100 28 35
    WS132 30 36
    WS132-10 27 37
    WS132-100 30 41
    SG132 29 40
    SG132-10 28 38
    SG132-100 28 37
    SG132-10-US 25 42
    SG132-100-US 21 34
  • Each sample was placed on a zero background holder and placed in a Phillips PW 1800 diffractometer using Cu radiation. Scans were then run over the range of 5° to 50° with a step size of 0.05° and a counting time of 2 hours each.
  • Once the diffraction patterns was obtained, the phases were identified with the aid of the Powder Diffraction File published by the International Centre for Diffraction Data. In all samples the crystalline phase identified was cellulose - Ia, which has a triclinic structure.
  • The distinguishing feature among the 20 samples is the peak breadth, which is related to the crystallite domain size. The experimental peak breadth was used to compute the domain size and percent crystallinity and are reported in Table 4.
  • Percent crystallinity (Xc %) is measured as a ratio of the crystalline area to the total area under the x-ray diffraction peaks, X c % = A c A a + A c × 100 %
    Figure imgb0006

    where,
    • Ac = Area of crystalline phase
    • Aa = Area of amorphous phase
    • Xc = Percent of crystallinity
  • To determine the percent crystallinity for each sample it was necessary to first extract the amount of the amorphous phase. This is done by estimating the area of each diffraction pattern that can be attributed to the crystalline phase (represented by the sharper peaks) and the non-crystalline phase (represented by the broad humps beneath the pattern and centered at 22° and 38°).
  • A systematic process was used to minimize error in these calculations due to broad crystalline peaks as well as high background intensity, First, a linear background was applied and then removed. Second, two Gaussian peaks centered at 22° and 38° with widths of 10-12° each were fitted to the humps beneath the crystalline peaks. Third, the area beneath the two broad Gaussian peaks and the rest of the pattern were determined. Finally, percent crystallinity was calculated by dividing the area beneath the crystalline peak by the total intensity (after background subtraction). Domain size and % crystallinity of the samples as determined by X-ray diffraction (XRD) are presented in Table 4.
  • Example 11 - Porosimetry Analysis of Irradiated Materials
  • Mercury pore size and pore volume analysis (Table 5) is based on forcing mercury (a non-wetting liquid) into a porous structure under tightly controlled pressures. Since mercury does not wet most substances and will not spontaneously penetrate pores by capillary action, it must be forced into the voids of the sample by applying external pressure. The pressure required to fill the voids is inversely proportional to the size of the pores. Only a small amount of force or pressure is required to fill large voids, whereas much greater pressure is required to fill voids of very small pores. Table 5. Pore Size and Volume Distribution by Mercury Porosimetry
    Sample ID Total Intrusion Volume (mL/g) Total Pore Area (m2/g) Median Pore Diameter (Volume) (µm) Median Pore Diameter (Area) (µm) Average Pore Diameter (4V/A) (µm) Bulk Density @ 0.50 psig (g/mL) Apparent (skeletal) Density (g/mL) Porosity (%)
    P132 6.0594 1.228 36.2250 13.7278 19.7415 0.1448 1.1785 87.7163
    P132-10 5.5436 1.211 46.3463 4.5646 18.3106 0.1614 1.3355 89.4875
    P132-300 5.3985 0.998 34.5235 18.2005 21.6422 0.1612 1.2413 87.0151
    P132-181 3.2866 0.868 25.3448 12.2410 15.1509 0.2497 13916 82.0577
    P132-US 6.0005 14.787 98.3459 0.0055 1.6231 0.1404 0.8894 84.2199
    A132 2.0037 11.759 64.6308 0.0113 0.6816 0.3683 1.4058 73.7990
    A132-10 1.9514 10.326 53.2706 0.0105 0.7560 0.3768 1.4231 73.5241
    A132-100 1.9394 10.205 43.8966 0.0118 0.7602 0.3760 1.3889 72.9264
    SG132 2.5267 8.265 57.6958 0.0141 1.2229 0.3119 1.4708 78.7961
    SG132-10 2.1414 8.643 26.4666 0.0103 0.9910 0.3457 1.3315 74.0340
    SG132-100 2.5142 10.766 32.7118 0.0098 0.9342 0.3077 1.3590 77.3593
    SG132-10-US 4.4043 1.722 71.5734 1.1016 10.2319 0.1930 1.2883 85.0169
    SG132-100-US 4.9665 7.358 24.8462 0.0089 2.6998 0.1695 1.0731 84.2010
    WS132 2.9920 5.447 76.3675 0.0516 2.1971 0.2773 1.6279 82.9664
    WS132-10 3.1138 2.901 57.4727 0.3630 4.2940 0.2763 1.9808 86.0484
    WS132-100 3.2077 3.114 52.3284 0.2876 4.1199 0.2599 1.5611 83.3538
  • The AutoPore 9520 can attain a maximum pressure of 414 MPa or 60,000 psia. There are four low pressure stations for sample preparation and collection of macropore data from 0.2 psia to 50 psia. There are two high pressure chambers which collects data from 25 psia to 60,000 psia. The sample is placed in a bowl-like apparatus called a penetrometer, which is bonded to a glass capillary stem with a metal coating. As mercury invades the voids in and around the sample, it moves down the capillary stem. The loss of mercury from the capillary stem results in a change in the electrical capacitance. The change in capacitance during the experiment is converted to volume of mercury by knowing the stem volume of the penetrometer in use. A variety of penetrometers with different bowl (sample) sizes and capillaries are available to accommodate most sample sizes and configurations. Table 6 below defines some of the key parameters calculated for each sample. Table 6. Definition of Parameters
    Parameter Description
    Total Intrusion Volume: The total volume of mercury intruded during an experiment. This can include interstitial filling between small particles, porosity of sample, and compression volume of sample.
    Total Pore Area: The total intrusion volume converted to an area assuming cylindrical shaped pores.
    Median Pore Diameter (volume): The size at the 50th percentile on the cumulative volume graph.
    Median Pore Diameter (area): The size at the 50th percentile on the cumulative area graph.
    Average Pore Diameter: The total pore volume divided by the total pore area (4V/A).
    Bulk Density: The mass of the sample divided by the bulk volume. Bulk volume is determined at the filling pressure, typically 0.5 psia.
    Apparent Density: The mass of sample divided by the volume of sample measured at highest pressure, typically 60,000 psia.
    Porosity: (Bulk Density/ Apparent Density) x 100%
  • Example 12- Particle Size Analysis of Irradiated Materials
  • The technique of particle sizing by static light scattering is based on Mie theory (which also encompasses Fraunhofer theory). Mie theory predicts the intensity vs. angle relationship as a function of the size for spherical scattering particles provided that other system variables are known and held constant. These variables are the wavelength of incident light and the relative refractive index of the sample material. Application ofMie theory provides the detailed particle size information. Table 7 summarizes particle size using median diameter, mean diameter, and modal diameter as parameters. Table 7. Particle Size by Laser light Scattering (Dry Sample Dispersion)
    Sample ID Median Diameter (µm) Mean Diameter (µm) Modal Diameter (µm)
    A132 380.695 418.778 442.258
    A132-10 321.742 366.231 410.156
    A132-100 301.796 348.633 444.169
    SG132 369.400 411.790 455.508
    SG132-10 278.793 325.497 426.717
    SG132-100 242.757 298.686 390.097
    WS132 407.335 445.618 467.978
    WS132-10 194.237 226.604 297.941
    WS132-100 201.975 236.037 307.304
  • Particle size was determined by Laser Light Scattering (Dry Sample Dispersion) using a Malvern Mastersizer 2000 using the following conditions:
    Feed Rate: 35%
    Disperser Pressure: 4 Bar
    Optical Model: (2.610, 1.000i) 1.000
  • An appropriate amount of sample was introduced onto a vibratory tray. The feed rate and air pressure were adjusted to ensure that the particles were properly dispersed. The key component is selecting an air pressure that will break up agglomerations, but does not compromise the sample integrity. The amount of sample needed varies depending on the size of the particles. In general, samples with fine particles require less material than samples with coarse particles.
  • Example 13 - Surface Area Analysis of Irradiated Materials Table 8. Summary of Surface Area by Gas Adsorption
  • Surface area of each sample was analyzed using a Micromeritics ASAP 2420 Accelerated Surface Area and Porosimetry System. The samples were prepared by first degassing for 16 hours at 40 °C. Next, free space (both warm and cold) with helium is calculated and then the sample tube is evacuated again to remove the helium. Data collection begins after this second evacuation and consists of defining target pressures which controls how much gas is dosed onto the sample. At each target pressure, the quantity of gas adsorbed and the actual pressure are determined and recorded. The pressure inside the sample tube is measured with a pressure transducer. Additional doses of gas will continue until the target pressure is achieved and allowed to equilibrate. The quantity of gas adsorbed is determined by summing multiple doses onto the sample. The pressure and quantity define a gas adsorption isotherm and are used to calculate a number of parameters, including BET surface area (Table 8).
    Sample ID Single point surface area (m2/g) BET Surface Area (m2/g)
    P131 @ P/Po= 0.250387771 1.5253 1.6897
    P132-10 @ P/Po= 0.239496722 1.0212 1.2792
    P132-100 @ P/Po= 0.240538100 1.0338 12622
    P132-191 @ P/Po= 0.239166091 0.5102 0.6448
    P132-US @ P/Po= 0.217359072 1.0993 1.6793
    A132 @ P/Po= 0.240040610 0.5400 0.7614
    A132-10 @ P/Po= 0.211218936 0.5383 0.7212
    A132-100 @P/Po= 0.238791097 0.4258 0.5538
    SG132 @ P/Po= 0.237989353 0.6359 0.8350
    SG132-10 @ P/Po= 0.238576905 0.6794 0.8689
    SG132-100 @ P/Po= 0.241960361 0.5518 0.7034
    SG132-10-US @ P/Po= 0.225692889 0.5693 0.7510
    SG132-100-US @ P/Po= 0.225935246 1.0983 1.4963
    WS132 @ P/Po= 0.237823664 0.6582 0.8663
    WS132-10 @ P/Po= 0.238612476 0.6191 0.7912
    WS132-100 @ P/Po= 0.238398832 0.6255 0.8143
  • The BET model for isotherms is a widely used theory for calculating the specific surface area. The analysis involves determining the monolayer capacity of the sample surface by calculating the amount required to cover the entire surface with a single densely packed layer of krypton. The monolayer capacity is multiplied by the cross sectional area of a molecule of probe gas to determine the total surface area. Specific surface area is the surface area of the sample aliquot divided by the mass of the sample.
  • Example 14 - Fiber Length Determination of Irradiated Materials
  • Fiber length distribution testing was performed in triplicate on the samples submitted using the Techpap MorFi LB01 system. The average length and width are reported in Table 9. Table 9. Summary of Lignocellulosic Fiber Length and Width Data
    Sample ID Arithmetic Average (mm) Average Length weighted in Length (mm) Statistical Corrected Average Length Weighted in Length (mm) Width (micrometers)
    P132-10 0.484 0.615 0.773 24.7
    P132-100 0.369 0.423 0.496 23.8
    P132-181 0.312 0.342 0.392 24.4
    A132-10 0.382 0.423 0.650 43.2
    A132-100 0.362 0.435 0.592 29.9
    SG132-10 0.328 0.363 0.521 44.0
    SG132-100 0.325 0.351 0.466 43.8
    WS132-10 0.353 0.381 0.565 44.7
    WS132-100 0.354 0.371 0.536 45.4
  • Example 15 - Ultrasonic Treatment of Irradiated and Un-irradiated Switcthgrass
  • Switchgrass was sheared according to Example 4. The switchgrass was treated by ultrasound alone or irradiation with 10 Mrad or 100 Mrad of gamma rays, and then sonicated. The resulting materials correspond to G132-BR (un-irradiated), G132-10-BR (10 Mrad and sonication) and G132-100-BR (100 Mrad and sonication), as presented in Table 1. Sonication was performed on each sample for 30 minutes using 20kHz ultrasound from a 1000W horn under re-circulating conditions. Each sample was dispersed in water at a concentration of about 0.10 g/mL.
  • FIGS. 30 and 31 show the apparatus used for sonication. Apparatus 500 includes a converter 502 connected to booster 504 communicating with a horn 506 fabricated from titanium or an alloy of titanium. The horn, which has a seal 510 made from VITON® about its perimeter on its processing side, forms a liquid tight seal with a processing cell 508. The processing side of the horn is immersed in a liquid, such as water, that has dispersed therein the sample to be sonicated. Pressure in the cell is monitored with a pressure gauge 512. In operation, each sample is moved by pump 517 from tank 516 through the processing cell and is sonicated. After, sonication, the sample is captured in tank 520. The process can be reversed in that the contents of tank 520 can be sent through the processing cell and captured in tank 516.
  • This process can be repeated a number of times until a desired level of processing is delivered to the sample.
  • Example 18 - Scanning Electron Micrographs of Un-irradiated Switchgrass in Comparison to irradiated and Irradiated and Sonicated Switchgrass
  • Switchgrass samples for the scanning electron micrographs were applied to carbon tape and gold sputter coated (70 seconds). Images were taken with a JEOL 6500 field emission scanning electron microscope.
  • FIG. 32 is a scanning electron micrograph at 1000 X magnification of a fibrous material produced from shearing switchgrass on a rotary knife cutter, and then passing the sheared material through a 1/32 inch screen.
  • FIGS. 33 and 34 are scanning electron micrographs of the fibrous material of FIG. 32 after irradiation with 10 Mrad and 100 Mrad gamma rays, respectively, at 1000 X magnification.
  • FIG. 35 is a scanning electron micrographs of the fibrous material of FIG. 32 after irradiation with 10 Mrad and sonicaiton at 1000 X magnification.
  • FIG. 36 is a scanning electron micrographs of the fibrous material of FIG. 32 after irradiation with 100 Mrad and sonicaiton at 1000 X magnification.
  • Example 17 - Infrared Spectrum of Irradiated Kraft Paper In Comparison to Un-irradiated Kraft Paper
  • The FT-IR analysis was performed on a Nicolet/Impact 400. The results indicate that all samples reported in Table 1 are consistent with a cellulose-based material.
  • FIG 37 is an infrared spectrum of Kraft board paper sheared according to Example 4, while FIG. 38 is an infrared spectrum of the Kraft paper of FIG 38 after irradiation with 100 Mrad of gamma radiation. The irradiated sample shows an additional peak in region A (centered about 1730 cm-1) that is not found in the un-irradiated material.
  • Example 18 - Combination of Electron Beam and Sonication Pretreatment
  • Switchgrass is used as the feedstock and is sheared with a Munson rotary knife cutter into a fibrous material. The fibrous material is then evenly distributed onto an open tray composed of tin with an area of greater than about 500 in2. The fibrous material is distributed so that it has a depth of about 1- 2 inches in the open tray. The fibrous material may be distributed in plastic bags at lower doses of irradiation (under 10 MRad), and left uncovered on the metal tray at higher doses of radiation.
  • Separate samples of the fibrous material are then exposed to successive doses of electron beam radiation to achieve a total dose of 1 Mrad, 2 Mrad, 3, Mrad, 5 Mrad, 10 Mrad, 50 Mrad, and 100 Mrad. Some samples are maintained under the same conditions as the remaining samples, but are not irradiated, to serve as controls. After cooling, the irradiated fibrous material is sent on for further processing through a sonication device.
  • The sonication device includes a converter connected to booster communicating with a horn fabricated from titanium or an alloy of titanium. The horn, which has a seal made from VITON® about its perimeter on its processing side, forms a liquid tight seal with a processing cell. The processing side of the horn is immersed in a liquid, such as water, into which the irradiated fibrous material to be sonicated is immersed. Pressure in the cell is monitored with a pressure gauge. In operation, each sample is moved by pump through the processing cell and is sonicated.
  • To prepare the irradiated fibrous material for sonication, the irradiated fibrous material is removed from any container (e.g., plastic bags) and is dispersed in water at a concentration of about 0.10 g/mL. Sonication is performed on each sample for 30 minutes using 20 kHz ultrasound from a 1000 W horn under re-circulating conditions. After sonication, the irradiated fibrous material is captured in a tank. This process can be repeated a number of times until a desired level of processing is achieved based on monitoring the structural changes in the switchgrass. Again, some irradiated samples are kept under the same conditions as the remaining samples, but are not sonicated, to serve as controls. In addition, some samples that were not irradiated are sonicated, again to serve as controls. Thus, some controls are not processed, some are only irradiated, and some are only sonicated.
  • Example 19 - Microbial Testing of Pretreated Biomass
  • Specific lignocellulosic materials pretreated as described herein are analyzed for toxicity to common strains of yeast and bacteria used in the biofuels industry for the fermentation step in ethanol production. Additionally, sugar content and compatibility with cellulase enzymes are examined to determine the viability of the treatment process. Testing of the pretreated materials is carried out in two phases as follows.
  • I. Toxicity and Sugar Content
  • Toxicity of the pretreated grasses and paper feedstocks is measured in yeast Saccharomyces cerevisiae (wine yeast) and Pichia stipitis (ATCC 66278) as well as the bacteria Zymomonas mobilis (ATCC 31821) and Clostridium thermocellum (ATCC 31924). A growth study is performed with each of the organisms to determine the optimal time of incubation and sampling.
  • Each of the feedstocks is then incubated, in duplicate, with S. cerevisiae, P. stipitis, Z. mobilis, and C. thermocellum in a standard microbiological medium for each organism. YM broth is used for the two yeast strains, S. cerevisiae and P. stipitis. RM medium is used for Z. mobilis and CM4 medium for C. thermocellum. A positive control, with pure sugar added, but no feedstock, is used for comparison. During the incubation, a total of five samples is taken over a 12 hour period at time 0, 3, 6, 9, and 12 hours and analyzed for viability (plate counts for Z. mobilis and direct counts for S. cerevisiae) and ethanol concentration.
  • Sugar content of the feedstocks is measured using High Performance Liquid Chromatography (HPLC) equipped with either a Shodex™ sugar SP0810 or Biorad Aminex® HPX-87P column. Each of the feedstocks (approx. 5 g) is mixed with reverse osmosis (RO) water for 1 hour. The liquid portion of the mixture is removed and analyzed for glucose, galactose, xylose, mannose, arabinose, and cellobiose content. The analysis is performed according to National Bioenergy Center protocol Determination of Structural Carbohydrates and Lignin in Biomass.
  • II. Cellulase Compatibility
  • Feedstocks are tested, in duplicate, with commercially available Accellerase™ 1000, which contains a complex of enzymes that reduces lignocellulosic biomass into fermentable sugars."two different cellulase preparations, Trichoderma reesei and Aspergillus nidulans at the recommended temperature and concentration in an Erlenmeyer flask. The flasks are incubated with moderate shaking at around 200 rpm for 12 hours. During that time, samples are taken every three hours at time 0, 3, 6, 9, and 12 hours to determine the concentration of reducing sugars (Hope and Dean, Biotech J., 1974, 144:403) in the liquid portion of the flasks.
  • Example 20 - Alcohol Production Using irradiation-Sonication Pretreatment
  • The optimum size for biomass conversion plants is affected by factors including economies of scale and the type and availability of biomass used as feedstock. Increasing plant size tends to increase economies of scale associated with plant processes. However, increasing plant size also tends to increase the costs (e.g., transportation costs) per unit of biomass feedstock. Studies analyzing these factors suggest that the appropriate size for biomass conversion plants can range from 2000 to 10,000 dried tons of biomass feedstock per day. The plant described below is sized to process 2000 tons of dry biomass feedstock per day.
  • FIG. 39 shows a process schematic of a biomass conversion system configured to process switchgrass. The feed preparation subsystem processes raw biomass feedstock to remove foreign objects and provide consistently sized particles for further processing. The pretreatment subsystem changes the molecular structure (e.g., reduces the average molecular weight and the crystallinity) of the biomass feedstock by irradiating the biomass feedstock, mixing the irradiated the biomass feedstock with water to form a slurry, and applying ultrasonic energy to the slurry. The irradiation and sonication convert the cellulosic and lignocellulosic components of the biomass feedstock into fermentable materials. The primary process subsystem ferments the glucose and other low weight sugars present after pretreatment to form alcohols.
  • Feed preparation
  • The selected design feed rate for the plant is 2,000 dry tons per day of switchgrass biomass. The design feed is chopped and/or sheared switchgrass.
  • Biomass feedstock in the form of bales of switchgrass are received by the plant on truck trailers. As the trucks are received, they are weighed and unloaded by forklifts. Some bales are sent to on-site storage while others are taken directly to the conveyors. From there, the bales are conveyed to an automatic unwrapping system that cuts away the plastic wrapping and/or net surrounding the bales. The biomass feedstock is then conveyed past a magnetic separator to remove tramp metal, after which it is introduced to shredder-shearer trains where the material is reduced in size. Finally, the biomass feedstock is conveyed to the pretreatment subsystem.
  • In some cases, the switchgrass bales are wrapped with plastic net to ensure they don't break apart when handled, and may also be wrapped in plastic film to protect the bale from weather. The bales are either square or round. The bales are received at the plant from off-site storage on large truck trailers.
  • Since switchgrass is only seasonally available, long-term storage is required to provide feed to the plant year-round. Long-term storage will likely consist of 400-500 acres of uncovered piled rows of bales at a location (or multiple locations) reasonably close to the ethanol plant. On-site short-term storage is provided equivalent to 72 hours of production at an outside storage area. Bales and surrounding access ways as well as the transport conveyors will be on a concrete slab. A concrete slab is used because of the volume of traffic required to deliver the large amount of biomass feedstock required. A concrete slab will minimize the amount of standing water in the storage area, as well as reduce the biomass feedstock's exposure to dirt. The stored material provides a short-term supply for weekends, holidays, and when normal direct delivery of material into the process is interrupted.
  • The bales are off-loaded by forklifts and are placed directly onto bale transport conveyors or in the short-term storage area. Bales are also reclaimed from short-term storage by forklifts and loaded onto the bale transport conveyors.
  • Bales travel to one of two bale unwrapping stations. Unwrapped bales are broken up using a spreader bar and then discharged onto a conveyor which passes a magnetic separator to remove metal prior to shredding. A tramp iron magnet is provided to catch stray magnetic metal and a scalping screen removes gross oversize and foreign material ahead of multiple shredder-shearer trains, which reduce the biomass feedstock to the proper size for pretreatment. The shredder-shearer trains include shredders and rotary knife cutters. The shredders reduce the size of the raw biomass feedstock and feed the resulting material to the rotary knife cutters. The rotary knife cutters concurrently shear the biomass feedstock and screen the resulting material.
  • Three storage silos are provided to limit overall system downtime due to required maintenance on and/or breakdowns of feed preparation subsystem equipment. Each silo can hold approximately 55,000 cubic feet of biomass feedstock (~3 hours of plant operation).
  • Pretreatment
  • A conveyor belt carries the biomass feedstock from the feed preparation subsystem 110 to the pretreatment subsystem 114. As shown in FIG. 40, in the pretreatment subsystem 114, the biomass feedstock is irradiated using electron beam emitters, mixed with water to form a slurry, and subjected to the application of ultrasonic energy. As discussed above, irradiation of the biomass feedstock changes the molecular structure (e.g., reduces the average molecular weight and the crystallinity) of the biomass feedstock. Mixing the irradiated biomass feedstock into a slurry and applying ultrasonic energy to the slurry further changes the molecular structure of the biomass feedstock. Application of the radiation and sonication in sequence may have synergistic effects in that the combination of techniques appears to achieve greater changes to the molecular structure (e.g., reduces the average molecular weight and the crystallinity) than either technique can efficiently achieve on its own. Without wishing to be bound by theory, in addition to reducing the polymerization of the biomass feedstock by breaking intramolecular bonds between segments of cellulosic and lignocellulosic components of the biomass feedstock, the irradiation may make the overall physical structure of the biomass feedstock more brittle. After the brittle biomass feedstock is mixed into a slurry, the application of ultrasonic energy further changes the molecular structure (e.g., reduces the average molecular weight and the crystallinity) and also can reduce the size of biomass feedstock particles.
  • Electron Beam Irradiation
  • The conveyor belt 491 carrying the biomass feedstock into the pretreatment subsystem distributes the biomass feedstock into multiple feed streams (e.g., 50 feed streams) each leading to separate electron beam emitters 492. In this embodiment, the biomass feedstock is irradiated while it is dry. Each feed stream is carried on a separate conveyor belt to an associated electron beam emitter. Each irradiation feed conveyor belt can be approximately one meter wide. Before reaching the electron beam emitter, a localized vibration is induced in each conveyor belt to evenly distribute the dry biomass feedstock over the cross-sectional width of the conveyor belt.
  • Electron beam emitter 492 (e.g., electron beam irradiation devices commercially available from Titan Corporation, San Diego, CA) are configured to apply a 100 kilo-Gray dose of electrons applied at a power of 300 kW. The electron beam emitters are scanning beam devices with a sweep width of 1 meter to correspond to the width of the conveyor belt. In some embodiments, electron beam emitters with large, fixed beam widths are used. Factors including belt/beam width, desired dose, biomass feedstock density, and power applied govern the number of electron beam emitters required for the plant to process 2,000 tons per day of dry feed.
  • Sonication
  • The irradiated biomass feedstock is mixed with water to form a slurry before ultrasonic energy is applied. There can be a separate sonication system associated with each electron beam feed stream or several electron beam streams can be aggregated as feed for a single sonication system.
  • In each sonication system, the irradiated biomass feedstock is fed into a reservoir 1214 through a first intake 1232 and water is fed into the reservoir 1214 through second intake 1234. Appropriate valves (manual or automated) control the flow of biomass feedstock and the flow of water to produce a desired ratio of biomass feedstock to water (e.g., 10% cellulosic material, weight by volume). Each reservoir 1214 includes a mixer 1240 to agitate the contents of volume 1236 and disperse biomass feedstock throughout the water.
  • In each sonication system, the slurry is pumped (e.g., using a recessed impeller vortex pump 1218) from reservoir 1214 to and through a flow cell 1224 including an ultrasonic transducer 1226. In some embodiments, pump 1218 is configured to agitate the slurry 1216 such that the mixture of biomass feedstock and water is substantially uniform at inlet 1220 of the flow cell 1224. For example, the pump 1218 can agitate the slurry 1216 to create a turbulent flow that persists throughout the piping between the first pump and inlet 1220 of flow cell 1224.
  • Within the flow cell 1224, ultrasonic transducer 1226 transmits ultrasonic energy into slurry 1216 as the slurry flows through flow cell 1224. Ultrasonic transducer 1226 converts electrical energy into high frequency mechanical energy (e.g., ultrasonic energy) which is then delivered to the slurry through booster 48. Ultrasonic transducers are commercially available (e.g., from Hielscher USA, Inc. of Ringwood, New Jersey) that are capable of delivering a continuous power of 16 kilowatts.
  • The ultrasonic energy traveling through booster 1248 in reactor volume 1244 creates a series of compressions and rarefactions in process stream 1216 with an intensity sufficient to create cavitation in process stream 1216. Cavitation disaggregates components of the biomass feedstock including, for example, cellulosic and lignocellulosic material dispersed in process stream 1216 (e.g., slurry). Cavitation also produces free radicals in the water of process stream 1216 (e.g., slurry). These free radicals act to further break down the cellulosic material in process stream 1216. In general, about 250 MJ/m3 of ultrasonic energy is applied to process stream 1216 containing fragments of poplar chips. Other levels of ultrasonic energy (between about 5 and about 4000 MJ/m3, e.g., 10, 25, 50, 100, 250, 500, 750, 1000, 2000, or 3000) can be applied to other biomass feedstocks After exposure to ultrasonic energy in reactor volume 1244, process stream 1216 exits flow cell 24 through outlet 1222.
  • Flow cell 1224 also includes a heat exchanger 1246 in thermal communication with at least a portion of reactor volume 1244. Cooling fluid 1248 (e.g., water) flows into heat exchanger 1246 and absorbs heat generated when process stream 1216 (e.g., slurry) is sonicated in reactor volume 1244. In some embodiments, the flow of cooling fluid 1248 into heat exchanger 1246 is controlled to maintain an approximately constant temperature in reactor volume 1244. In addition or in the alternative, the temperature of cooling fluid 1248 flowing into heat exchanger 1246 is controlled to maintain an approximately constant temperature in reactor volume 1244.
  • The outlet 1242 of flow cell 1224 is arranged near the bottom of reservoir 1214 to induce a gravity feed of process stream 1216 (e.g., slurry) out of reservoir 1214 towards the inlet of a second pump 1230 which pumps process stream 1216 (e.g., slurry) towards the primary process subsystem.
  • Sonication systems can include a single flow path (as described above) or multiple parallel flow paths each with an associated individual sonication units. Multiple sonication units can also be arranged to series to increase the amount of sonic energy applied to the slurry.
  • Primary Processes
  • A vacuum rotary drum type filter removes solids from the slurry before fermentation. Liquid from the filter is pumped cooled prior to entering the fermentors. Filtered solids are passed to passed to the post-processing subsystem for further processing.
  • The fermentation tanks are large, low pressure, stainless steel vessels with conical bottoms and slow speed agitators. Multiple first stage fermentation tanks can be arranged in series. The temperature in the first stage fermentation tanks is controlled to 30 degrees centigrade using external heat exchangers. Yeast is added to the first stage fermentation tank at the head of each series of tanks and carries through to the other tanks in the series.
  • Second stage fermentation consists of two continuous fermentors in series. Both fermentors are continuously agitated with slow speed mechanical mixers. Temperature is controlled with chilled water in external exchangers with continuous recirculation. Recirculation pumps are of the progressive cavity type because of the high solids concentration.
  • Off gas from the fermentation tanks and fermentors is combined and washed in a counter-current water column before being vented to the atmosphere. The off gas is washed to recover ethanol rather than for air emissions control.
  • Post-Processing Distillation
  • Distillation and molecular sieve adsorption are used to recover ethanol from the raw fermentation beer and produce 99.5% ethanol. Distillation is accomplished in two columns-the first, called the beer column, removes the dissolved CO2 and most of the water, and the second concentrates the ethanol to a near azeotropic composition.
  • All the water from the nearly azeotropic mixture is removed by vapor phase molecular sieve adsorption. Regeneration of the adsorption columns requires that an ethanol water mixture be recycled to distillation for recovery.
  • Fermentation vents (containing mostly CO2, but also some ethanol) as well as the beer column vent are scrubbed in a water scrubber, recovering nearly all of the ethanol. The scrubber effluent is fed to the first distillation column along with the fermentation beer.
  • The bottoms from the first distillation contain all the unconverted insoluble and dissolved solids. The insoluble solids are dewatered by a pressure filter and sent to a combustor. The liquid from the pressure filter that is not recycled is concentrated in a multiple effect evaporator using waste heat from the distillation. The concentrated syrup from the evaporator is mixed with the solids being sent to the combustor, and the evaporated condensate is used as relatively clean recycle water to the process.
  • Because the amount of stillage water that can be recycled is limited, an evaporator is included in the process. The total amount of the water from the pressure filter that is directly recycled is set at 25%. Organic salts like ammonium acetate or lactate, steep liquor components not utilized by the organism, or inorganic compounds in the biomass end up in this stream. Recycling too much of this material can result in levels of ionic strength and osmotic pressures that can be detrimental to the fermenting organism's efficiency. For the water that is not recycled, the evaporator concentrates the dissolved solids into a syrup that can be sent to the combustor, minimizing the load to wastewater treatment.
  • Wastewater Treatment
  • The wastewater treatment section treats process water for reuse to reduce plant makeup water requirements. Wastewater is initially screened to remove large particles, which are collected in a hopper and sent to a landfill. Screening is followed by anaerobic digestion and aerobic digestion to digest organic matter in the stream. Anaerobic digestion produces a biogas stream that is rich in methane that is fed to the combustor. Aerobic digestion produces a relatively clean water stream for reuse in the process as well as a sludge that is primarily composed of cell mass. The sludge is also burned in the combustor. This screening / anaerobic digestion / aerobic digestion scheme is standard within the current ethanol industry and facilities in the 1-5 million gallons per day range can be obtained as "off-the-shelf" units from vendors.
  • Combustor, Boiler, and Turbogenerator
  • The purpose of the combustor, boiler, and turbogenerator subsystem is to burn various by-product streams for steam and electricity generation. For example, some lignin, cellulose, and hemicellulose remains unconverted through the pretreatment and primary processes. The majority of wastewater from the process is concentrated to a syrup high in soluble solids. Anaerobic digestion of the remaining wastewater produces a biogas high in methane. Aerobic digestion produces a small amount of waste biomass (sludge). Burning these by-product streams to generate steam and electricity allows the plant to be self sufficient in energy, reduces solid waste disposal costs, and generates additional revenue through sales of excess electricity.
  • Three primary fuel streams (post-distillate solids, biogas, and evaporator syrup) are fed to a circulating fluidized bed combustor. The small amount of waste biomass (sludge) from wastewater treatment is also sent to the combustor. A fan moves air into the combustion chamber. Treated water enters the heat exchanger circuit in the combustor and is evaporated and superheated to 510°C (950°F) and 86 atm (1265 psia) steam. Flue gas from the combustor preheats the entering combustion air then enters a baghouse to remove particulates, which are landfilled. The gas is exhausted through a stack.
  • A multistage turbine and generator are used to generate electricity. Steam is extracted from the turbine at three different conditions for injection into the pretreatment reactor and heat exchange in distillation and evaporation. The remaining steam is condensed with cooling water and returned to the boiler feedwater system along with condensate from the various heat exchangers in the process. Treated well water is used as makeup to replace steam used in direct injection.
  • OTHER EMBODIMENTS
  • A number of embodiments of the invention have been described. Nevertheless, it will be understood that various modifications may be made without departing from the spirit and scope of the invention.
  • In some embodiments, relatively low doses of radiation, optionally, combined with acoustic energy, e.g., ultrasound, are utilized to crosslink, graft, or otherwise increase the molecular weight of a natural or synthetic carbohydrate-containing material, such as any of those materials in any form (e.g., fibrous form) described herein, e.g., sheared or un-sheared cellulosic or lignocellulosic materials, such as cellulose. The crosslinking, grafting, or otherwise increasing the molecular weight of the natural or synthetic carbohydrate-containing material can be performed in a controlled and predetermined manner by selecting the type or types of radiation employed (e.g., e-beam and ultraviolet or e-beam and gamma) and/or dose or number of doses of radiation applied. Such a material having increased molecular weight can be useful in making a composite, such as a fiber-resin composite, having improved mechanical properties, such as abrasion resistance, compression strength, fracture resistance, impact strength, bending strength, tensile modulus, flexural modulus and elongation at break. Crosslinking, grafting, or otherwise increasing the molecular weight of a selected material can improve the thermal stability of the material relative to an un-treated material. Increasing the thermal stability of the selected material can allow it to be processed at higher temperatures without degradation In addition, treating materials with radiation can sterilize the materials, which can reduce their tendency to rot, e.g., while in a composite. The crosslinking, grafting, or otherwise increasing the molecular weight of a natural or synthetic carbohydrate-containing material can be performed in a controlled and predetermined manner for a particular application to provide optimal properties, such as strength, by selecting the type or types of radiation employed and/or dose or doses of radiation applied.
  • When used, the combination of radiation, e.g., low dose radiation, and acoustic energy, e.g., sonic or ultrasonic energy, can improve material throughput and/or minimize energy usage.
  • The resin can be any thermoplastic, thermoset, elastomer, adhesive, or mixtures of these resins. Suitable resins include any resin, or mixture of resins described herein.
  • In addition to the resin alone, the material having the increased molecular weight can be combined, blended, or added to other materials, such as metals, metal alloys, ceramics (e.g., cement), lignin, elastomers, asphalts, glass, or mixtures of any of these and/or resins. When added to cement, fiber-reinforced cements can be produced having improved mechanical properties, such as the properties described herein, e.g., compression strength and/or fracture resistance.
  • Crosslinking, grafting, or otherwise increasing the molecular weight of a natural or synthetic carbohydrate-containing material utilizing radiation can provide useful materials in many forms and for many applications. For example, the carbohydrate-containing material can be in the form of a paper product, such as paper, paper pulp, or paper effluent, particle board, glued lumber laminates, e.g., veneer, or plywood, lumber, e.g., pine, poplar, oak, or even balsa wood lumber. Treating paper, particle board, laminates or lumber, can increase their mechanical properties, such as their strength. For example, treating pine lumber with radiation can make a high strength structural material.
  • When paper is made using radiation, radiation can be utilized at any point in its manufacture. For example, the pulp can be irradiated, a pressed fiber preform can be irradiated, or the finished paper itself can be irradiated. In some embodiments, radiation is applied at more than one point during the manufacturing process..
  • For example, a fibrous material that includes a first cellulosic and/or lignocellulosic material having a first molecular weight can be irradiated in a manner to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight. For example, if gamma radiation is utilized as the radiation source, a dose of from about 0.2 Mrad to about 10 Mrad, e.g., from about 0.5 Mrad to about 7.5 Mrad, or from about 2.0 Mrad to about 5.0 Mrad, can be applied. If e-beam radiation is utilized, a smaller dose can be utilized (relative to gamma radiation), such as a dose of from about 0.1 Mrad to about 5 Mrad, e.g., between about 0.2 Mrad to about 3 Mrad, or between about 0.25 Mrad and about 2.5 Mrad. After the relatively low dose of radiation, the second cellulosic and/or lignocellulosic material can be combined with a material, such as a resin, and formed into a composite, e.g., by compression molding, injection molding or extrusion. Forming resin-fiber composites is described in WO 2006/102543 . Once composites are formed, they can be irradiated to further increase the molecular weight of the carbohydrate-containing material while in the composite.
  • Alternatively, a fibrous material that includes a first cellulosic and/or lignocellulosic material having a first molecular weight can be combined with a material, such as a resin, to provide a composite, and then the composite can be irradiated with a relatively low dose of radiation so as to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight For example, if gamma radiation is utilized as the radiation source, a dose of from about 1 Mrad to about 10 Mrad can be applied. Using this approach increases the molecular weight of the material while it is with a matrix, such as a resin matrix. In some embodiments, the resin is a cross-linkable resin, and, as such, it crosslinks as the carbohydrate-containing material increases in molecular weight, which can provide a synergistic effect to provide maximum mechanical properties to a composite. For example, such composites can have excellent low temperature performance, e.g., having a reduced tendency to break and/or crack at low temperatures, e.g., temperatures below 0 °C, e.g., below -10 °C, -20 °C, -40 °C, -50 °C, -60 °C or even below -100 °C, and/or excellent performance at high temperatures, e.g., capable of maintaining their advantageous mechanical properties at relatively high temperature, e.g., at temperatures above 100 °C, e.g., above 125 °C, 150 °C, 200 °C, 250 °C, 300 °C, 400 °C, or even above 500 °C. In addition, such composites can have excellent chemical resistance, e.g., resistance to swelling in a solvent, e.g., a hydrocarbon solvent, resistance to chemical attack, e.g., by strong acids, strong bases, strong oxidants (e.g., chlorine or bleach) or reducing agents (e.g., active metals such as sodium and potassium).
  • In some embodiments, the resin, or other matrix material, does not crosslink during irradiation. In some embodiments, additional radiation is applied while the carbohydrate-containing material is within the matrix to further increase the molecular weight of the carbohydrate-containing material. In some embodiments, the radiation causes bonds to form between the matrix and the carbohydrate-containing material.
  • In some embodiments, the carbohydrate-containing material is in the form of fibers. In such embodiments, when the fibers are utilized in a composite, the fibers can be randomly oriented within the matrix. In other embodiments, the fibers can be substantially oriented, such as in one, two, three or four directions. If desired, the fibers can be continuous or discrete.
  • Any of the following additives can added to the fibrous materials, densified fibrous materials a or any other materials and composites described herein. Additives, e.g., in the form of a solid, a liquid or a.gas, can be added, e.g., to the combination of a fibrous material and resin. Additives include fillers such as calcium carbonate, graphite, wollastonite, mica, glass, fiber glass, silica, and talc; inorganic flame retardants such as alumina trihydrate or magnesium hydroxide; organic flame retardants such as chlorinated or brominated organic compounds; ground construction waste; ground tire rubber, carbon fibers; or metal fibers or powders (e.g., aluminum, stainless steel). These additives can reinforce, extend, or change electrical, mechanical or compatibility properties. Other additives include lignin, fragrances, coupling agents, compatibilizers, e.g., maleated polypropylene, processing aids, lubricants, e.g., fluorinated polyethylene, plasticizers, antioxidants, opacifiers, heat stabilizers, colorants, foaming agents, impact modifiers, polymers, e.g., degradable polymers, photostabilizers, biocides, antistatic agents, e.g., stearates or ethoxylated fatty acid amines. Suitable antistatic compounds include conductive carbon blacks, carbon fibers, metal fillers, cationic compounds, e.g., quaternary ammonium compounds, e.g., N-(3-chloro-2-hydroxypropyl)-trimethylammonium chloride, alkanolamides, and amines. Representative degradable polymers include polyhydroxy acids, e.g., polylactides, polyglycolides and copolymers of lactic acid and glycolic acid, poly(hydroxybutyric acid), poly(hydroxyvaleric acid), poly[lactide-co-(e-caprolactone)], poly[glycolide-co-(e-caprolactone)], polycarbonates, poly(amino acids), poly(hydroxyalkanoate)s, polyanhydrides, polyorthoesters and blends of these polymers.
  • When described additives are included, they can be present in amounts, calculated on a dry weight basis, of from below 1 percent to as high as 80 percent, based on total weight of the fibrous material. More typically, amounts range from between about 0.5 percent to about 50 percent by weight, e.g., 5 percent, 10 percent, 20 percent, 30, percent or more, e.g., 40 percent.
  • Any additives described herein can be encapsulated, e.g., spray dried or microencapsulated, e.g., to protect the additives from heat or moisture during handling.
  • The fibrous materials, densified fibrous materials, resins or additives may be dyed. For example, the fibrous material can be dyed before combining with the resin and compounding to form composites. In some embodiments, this dyeing can be helpful in masking or hiding the fibrous material, especially large agglomerations of the fibrous material, in molded or extruded parts, when this is desired. Such large agglomerations, when present in relatively high concentrations, can show up as speckles in the surfaces of the molded or extruded parts.
  • For example, the desired fibrous material can be dyed using an acid dye, direct dye or a reactive dye. Such dyes are available from Spectra Dyes, Kearny, NJ or Keystone Aniline Corporation, Chicago, IL. Specific examples of dyes include SPECTRA™ LIGHT YELLOW 2G, SPECTRACID™ YELLOW 4GL CONC 200, SPECTRANYL™ RHODAMINE 8, SPECTRANYL™ NEUTRAL RED B, SPECTRAMINE™ BENZOPERPURINE, SPECTRADIAZO™ BLACK OB, SPECTRAMINE™ TURQUOISE G, and SPECTRAMINE™ GREY LVL 200%, each being available from Spectra Dyes.
  • In some embodiments, resin color concentrates containing pigments are blended with dyes. When such blends are then compounded with the desired fibrous material, the fibrous material may be dyed in-situ during the compounding. Color concentrates are available from Clariant.
  • It can be advantageous to add a scent or fragrance to the fibrous materials, densified fibrous or composites. For example, it can be advantageous for the composites smell and/or look like natural wood, e.g., cedarwood. For example, the fragrance, e.g., natural wood fragrance, can be compounded into the resin used to make the composite. In some implementations, the fragrance is compounded directly into the resin as an oil. For example, the oil can be compounded into the resin using a roll mill, e.g., a Banbury® mixer or an extruder, e.g., a twin-screw extruder with counter-rotating screws. An example of a Banbury® mixer is the F-Series Banbury® mixer, manufactured by Farrel. An example of a twin-screw extruder is the WP ZSK 50 MEGAcompunder, manufactured by Krupp Wemer & Pfleiderer. After compounding, the scented resin can be added to the fibrous material and extruded or molded. Alternatively, master batches of fragrance-filled resins are available commercially from International Flavors and Fragrances, under the tradename PolyIff or from the RTP Company. In some embodiments, the amount of fragrance in the composite is between about 0.005 % by weight and about 10 % by weight, e.g., between about 0.1 % and about 5 % or 0.25 % and about 2.5 %.
  • Other natural wood fragrances include evergreen or redwood. Other fragrances include peppermint, cherry, strawberry, peach, lime, spearmint, cinnamon, anise, basil, bergamot, black pepper, camphor, chamomile, citronella, eucalyptus, pine, fir, geranium, ginger, grapefruit, jasmine, juniperberry, lavender, lemon, mandarin, marjoram, musk, myrhh, orange, patchouli, rose, rosemary, sage, sandalwood, tea tree, thyme, wintergreen, ylang ylang, vanilla, new car or mixtures of these fragrances. In some embodiments, the amount of fragrance in the fibrous material-fragrance combination is between about 0.005 % by weight and about 20 % by weight, e.g., between about 0.1 % and about 5 % or 0.25 % and about 2.5 %.
  • While fibrous materials have been described, such as cellulosic and lignocellulosic fibrous materials, other fillers may be used for making the composites. For example, inorganic fillers such as calcium carbonate (e.g., precipitated calcium carbonate or natural calcium carbonate), aragonite clay, orthorhombic clays, calcite clay, rhombohedral clays, kaolin, clay, bentonite clay, dicalcium phosphate, tricalcium phosphate, calcium pyrophosphate, insoluble sodium metaphosphate, precipitated calcium carbonate, magnesium orthophosphate, trimagnesium phosphate, hydroxyapatites, synthetic apatites, alumina, silica xerogel, metal aluminosilicate complexes, sodium aluminum silicates, zirconium silicate, silicon dioxide or combinations of the inorganic additives may be used. The fillers can have, e.g., a particle size of greater than 1 micron, e.g., greater than 2 micron, 5 micron, 10 micron, 25 micron or even greater than 35 microns.
  • Nanometer scale fillers can also be used alone, or in combination with fibrous materials of any size and/or shape. The fillers can be in the form of, e.g., a particle, a plate or a fiber. For example, nanometer sized clays, silicon and carbon nanotubes, and silicon and carbon nanowires can be used. The filler can have a transverse dimension less than 1000 nm, e.g., less than 900 nm, 800 nm, 750 nm, 600 nm, 500 nm, 350 nm, 300 nm, 250 nm, 200 nm, less than 100 nm, or even less than 50 nm.
  • In some embodiments, the nano-clay is a montmorillonite. Such clays are available from Nanocor, Inc. and Southern Clay products, and have been described in U.S. Patent Nos. 6,849,680 and 6,737,464 . The clays can be surface treated before mixing into, e.g., a resin or a fibrous material. For example, the clay can be surface is treated so that its surface is ionic in nature, e.g., cationic or anionic.
  • Aggregated or agglomerated nanometer scale fillers, or nanometer scale fillers that are assembled into supramolecular structures, e.g., self-assembled supramolecular structures can also be used. The aggregated or supramolecular fillers can be open or closed in structure, and can have a variety of shapes, e.g., cage, tube or spherical.
  • Accordingly, other embodiments are within the scope of the following claims.
  • Further aspects of the invention defined herein include the flowing.
    1. 1. A method of changing a molecular structure of a biomass feedstock, the method comprising preparing the biomass feedstock by reducing one or more dimensions of individual pieces of biomass; pretreating the biomass feedstock using two or more different pretreatment methods that each change the molecular structure, wherein the different pretreatment methods are selected from radiation, sonication, pyrolysis, and oxidation; and processing the prepared and pretreated biomass feedstock to produce a product.
    2. 2. The method of aspect 1, wherein the biomass feedstock is prepared and then pretreated.
    3. 3. The method of aspect 1, wherein the biomass feedstock is pretreated and then prepared.
    4. 4. The method of aspect 1, wherein reducing one or more dimensions of individual pieces of biomass comprises shearing.
    5. 5. The method of aspect 1, wherein the two or more pretreatment methods are applied to the biomass feedstock at or about the same time.
    6. 6. The method of aspect 1, wherein the two or more pretreatment methods comprise radiation and sonication.
    7. 7. The method of aspect 6, wherein the radiation is in the form of an electron beam.
    8. 8. The method of aspect 7, wherein the electron beam radiation is applied at a total dosage of about 10 MRad and the sonication is applied at a total energy of more than 5 MJ/m3.
    9. 9. The method of any one of aspects 6 to 8, wherein radiation precedes sonication.
    10. 10. The method of any one of aspects 6 to 8, wherein sonication precedes radiation.
    11. 11. The method of any one of aspects 6 to 8, wherein radiation and sonication are performed at or about the same time.
    12. 12. The method of aspect 1, wherein the change in molecular structure of the biomass feedstock comprises a change in any one or more of an average molecular weight, average crystallinity, surface area, polymerization, porosity, branching, grafting, and domain size or number of the biomass.
    13. 13. The method of aspect 1, wherein the change in molecular structure of the biomass feedstock comprises a decrease in either one or both of an average molecular weight and average crystallinity of the biomass or an increase in either one or both of surface area and porosity of the biomass.
    14. 14. A method of making a product, such as a combustible fuel, the method comprising: providing a material comprising a carbohydrate produced by a process comprising pretreating a biomass feedstock with any two or more of radiation, sonication, pyrolysis, and oxidation; and contacting the material with a microorganism having the ability to convert at least a portion, e.g., at least about 1 percent by weight, of the material to the product, such as the combustible fuel.
    15. 15. The method of any one of aspects 1 to 14, wherein the two or more different pretreatment methods comprise radiation and sonication, radiation and oxidation, radiation and pyrolization, sonication and oxidation, sonication and pyrolization, or oxidation and pyrolization.
    16. 16. The method of any one of the above aspects, further comprising pretreating the biomass feedstock with steam explosion.
    17. 17. The method of any one of the above aspects, wherein the process does not include hydrolyzing the biomass with an acid or a base.
    18. 18. The method of any one of the above aspects, wherein at least about seventy percent by weight of the biomass has not been hydrolyzed.
    19. 19. The method of any one of the above aspects, wherein at least at 95 percent by weight of the biomass has not been hydrolyzed.
    20. 20. The method of any one of the above aspects, wherein substantial none of the biomass has been hydrolyzed.
    21. 21. The method of any one of the above aspects, wherein at least one pretreatment method is performed on biomass in which less than about 25 percent by weight of the biomass is wetted with a liquid, such as water.
    22. 22. The method of any one of the above aspects, wherein at least one pretreatment method is performed on biomass in which substantially none of the biomass is wetted with a liquid, such as water.
    23. 23. The method of any one of the above aspects, wherein the biomass has less than about five percent by weight retained water, measured at 25°C and at fifty percent relative humidity.
    24. 24. The method of any one of the above aspects, wherein at least one pretreatment method is performed on biomass in which less than about 25 percent by weight of the biomass is in a swollen state, the swollen state being characterized as having a volume of more than about 2.5 percent higher than an unswollen state.
    25. 25. The method of any one of the above aspects, wherein the biomass is mixed with or includes a swelling agent.
    26. 26. The method of any one of the above aspects, wherein the biomass is mixed with or includes a swelling agent, and wherein the biomass receives a dose of less than about 10 Mrad of radiation.
    27. 27. The method of aspect 24, wherein one of the pretreatment methods is radiation.
    28. 28. The method of any one of the above aspects, wherein at least one of the pretreatment methods, e.g., radiation, is performed on the biomass feedstock while the biomass feedstock is exposed to air.
    29. 29. The method of any one of the above aspects, wherein at least one of the pretreatment methods, e.g., radiation, is performed on the biomass under a pressure of greater than about 2.5 atmospheres, such as greater than 5 or 10 atmospheres.
    30. 30. The method of any one of the above aspects, wherein the process further comprises oxidizing, pyrolizing, or steam exploding the biomass.
    31. 31. The method of any one of the above aspects, wherein the biomass feedstock is selected from the group consisting of paper, paper products, paper waste, wood, particle board, sawdust, agricultural waste, sewage, silage, grasses, rice hulls, bagasse, cotton, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, corn stover, switchgrass, alfalfa, hay, rice hulls, coconut hair, cotton, synthetic celluloses, seaweed, algae, and mixtures thereof.
    32. 32. The method of any one of the above aspects, wherein the biomass comprises a synthetic material.
    33. 33. The method of any one of the above aspects 14 to 32, wherein the fuel comprises one or more of hydrogen, alcohols, and hydrocarbons.
    34. 34. The method of aspect 33, wherein the alcohols are selected from the group consisting of ethanol, n-propanol, isoproanol, n-butanol, and mixtures thereof.
    35. 35. The method of any one of the above aspects 14 to 34, wherein the microorganism comprises a bacterium.
    36. 36. The method of any one of the above aspects 14 to 34, wherein the microorganism comprises a yeast.
    37. 37. The method of any one of the above aspects 14 to 36, wherein converting comprises fermenting the material to the product, such as the combustible fuel.
    38. 38. The method of any one of the above aspects, wherein the irradiation is performed utilizing an ionizing radiation, such as gamma rays, a beam of electrons, or ultraviolet C radiation having a wavelength of from about 100 ran to about 280 ran.
    39. 39. The method of aspect 38, wherein the ionizing radiation comprises electron beam radiation.
    40. 40. The method of aspect 38 or 39, wherein the radiation is applied at a total dose of between about 10 Mrad and about 150 Mrad, such as at a dose rate of about 0.5 to about 10 Mrad/day, or 1 Mrad/s to about 10 Mrad/s.
    41. 41. The method of any one of the above aspects wherein irradiating includes applying two or more radiation sources, such as gamma rays and a beam of electrons.
    42. 42. The method of any one of the above aspects, wherein sonication is performed at a frequency of between about 15 kHz and about 25 kHz, such as between about 18 kHz and 22 kHz.
    43. 43. The method of any one of the above aspects, wherein the biomass comprises a first cellulose having a first number average molecular weight and the carbohydrate material comprises a second cellulose having a second number average molecular weight lower than the first number average molecular weight.
    44. 44. The method of aspect 43, wherein the second number average molecular weight is lower than the first number average molecular weight by more than about one-fold.
    45. 45. The method of aspect 43 or 44, wherein the first cellulose has a first crystallinity and wherein the second cellulose has a second crystallinity lower than the first crystallinity.
    46. 46. The method of aspect 45, wherein the second crystallinity is lower than the first crystallinity by more than about 10 percent.
    47. 47. The method of any one of aspects 43 to 46, wherein the first cellulose has a first level of oxidation and wherein the second cellulose has a second level of oxidation higher than the first level of oxidation.
    48. 48. The method of any one of the above aspects, wherein the biomass feedstock is prepared by shearing a biomass fiber source to provide a fibrous material.
    49. 49. The method of aspect 48, wherein the shearing is performed with a rotary knife cutter.
    50. 50. The method of aspect 48 or 49, wherein fibers of the fibrous material have an average length-to-diameter ratio of greater than 5/1.
    51. 51. The method of any one of aspects 48 to 50, wherein the fibrous material has a BET surface area of greater than 0.25 m2/g.
    52. 52. The method of any one of the above aspects 14 to 51, wherein the carbohydrate comprises one or more β-1,4-linkages and having a number average molecular weight between about 3,000 and 50,000.
    53. 53. The method of any one of the above aspects, wherein the pretreated biomass material further comprises a buffer, such as sodium bicarbonate or ammonium chloride.
    54. 54. The method of any one of the above aspects, wherein the pretreated biomass material further comprises an eledrolyte, such as potassium chloride or sodium chloride.
    55. 55. The method of any one of the above aspects, wherein the pretreated biomass material further comprises a growth factor, such as biotin and/or a base pair such as uracil.
    56. 56. The method of any one of the above aspects, wherein the pretreated biomass material further comprises a surfactant.
    57. 57. The method of any one of the above aspects, wherein the pretreated biomass material further comprises a mineral.
    58. 58. The method of any one of the above aspects, wherein the pretreated biomass material further comprises a chelating agent.
    59. 59. The method of any one of the above aspects, wherein the biomass feedstock is pretreated using any three or more of radiation, sonication, pyrolysis, and oxidation, in any order, or at about the same time.
    60. 60. A method of making a product, such as a combustible fuel, the method comprising: providing a material comprising a carbohydrate produced by pretreating a biomass feedstock with any one or more of radiation, sonication, oxidation, pyrolysis, and steam explosion, wherein less than about 25 percent by weight of the biomass is in a swollen state, the swollen state being characterized as having a volume of more than about 2.5 percent higher than a nominal, unswollen state; and contacting the material with a microorganism having the ability to convert at least a portion, e.g., at least about 1 percent by weight, of the material to the product, such as the combustible fuel.
    61. 61. A method of making a product, such as a combustible fuel, the method comprising: providing a material comprising a carbohydrate produced by pretreating a biomass feedstock with any one or more of radiation, sonication, oxidation, pyrolysis, and steam explosion, wherein less than about 25 percent by weight of the biomass is hydrolyzed subsequent to pretreatment; and contacting the material with a microorganism having the ability to convert at least a portion of the material, e.g., at least about 1 percent by weight, to the product, such as the combustible fuel.
    62. 62. A method of making a product, such as a combustible fuel, the method comprising: providing a material comprising a carbohydrate produced by pretreating a biomass feedstock with any one or more of radiation, sonication, oxidation, pyrolysis, and steam explosion, wherein less than about 25 percent by weight of the biomass is in contact with a liquid, such as water, and contacting the material with a microorganism having the ability to convert at least a portion, e.g., at least about 1 percent by weight, of the material to the product, such as the combustible fuel.
    63. 63. The method of any one of aspects 60 to 62, wherein the method comprises selecting two or more different pretreatment methods.
    64. 64. The method of aspect 63, wherein the two or more different pretreatment methods comprise radiation and sonication, radiation and oxidation, radiation and pyrolization, sonication and oxidation, sonication and pyrolization, or oxidation and pyrolization.
    65. 65. The method of aspect 64, further comprising pretreating the biomass with steam explosion.
    66. 66. The method of any one of aspects 60 to 65, wherein the process does not include hydrolyzing the biomass with an acid or a base.
    67. 67. The method of any one of aspects 60 to 66, wherein the microorganism comprises a bacterium or yeast
    68. 68. The method of any one of aspects 60 to 67, wherein the irradiating is performed utilizing an ionizing radiation, such as gamma rays or a beam of electrons.
    69. 69. The method of aspect 68, wherein the ionizing radiation comprises electron beam radiation.
    70. 70. The method of aspect 62, wherein the liquid is water.
    71. 71. A method of making a product, such as a combustible fuel, the method comprising: providing a material comprising a carbohydrate produced by pretreating a sheared biomass feedstock with any one or more of radiation, sonication, oxidation, pyrolysis, and steam explosion; and contacting the material with a microorganism having the ability to convert at least a portion, e.g., at least about 1 percent by weight, of the material to the product, such as the combustible fuel.
    72. 72. The method of aspect 71, wherein the sheared biomass comprises discrete fibers having a length-to-diameter ratio (UD) of greater than about 5/1.
    73. 73. The method of aspect 71 or 72, wherein the biomass has internal fibers, and wherein the biomass has been sheared to an extent that its internal fibers are substantially exposed.
    74. 74. The method of any one of aspects 71 to 73, wherein the biomass has been sheared to an extent that it has a bulk density of less than about 0.35 g/cm3.
    75. 75. A biomass feedstock processing system comprising: a biomass feedstock preparation module for reducing size of pieces of biomass; two or more of the following pretreatment modules: a radiation module arranged to apply radiation to the biomass; a sonication module arranged to apply sonic energy to the biomass; an oxidation module arranged to oxidize the biomass; and a pyrolysis module arranged to apply heat to the biomass; and a biomass transportation subsystem to move the biomass to and between modules within the processing system;
      wherein the two or more pretreatment modules are arranged in series and/or are arranged to treat a portion of the biomass at about the same time.
    76. 76. The system of aspect 75, further comprising a vessel.
    77. 77. A system comprising a reaction vessel containing a pretreated biomass material comprising a carbohydrate, wherein the pretreated biomass material is produced by a method of any one of aspects 1 to 74.
    78. 78. The system of aspect 76 or 77, wherein the vessel also contains a microorganism in contact with the material, the microorganism having the ability to convert at least a portion of the material to a product, such as a combustible fuel.
    79. 79. The system of any one of aspects 76 to 78, wherein the vessel also contains an enzyme in contact with the material, the enzyme having the ability to react with at least a portion of the material.
    80. 80. The system of any one of aspects 76 to 79, wherein the vessel also contains a buffer, such as sodium bicarbonate or ammonium chloride.
    81. 81. The system of any one of aspects 76 to 80, wherein the vessel also contains an electrolyte, such as potassium chloride or sodium chloride.
    82. 82. The system of any one of aspects 76 to 81, wherein the vessel also contains a growth factor, such as biotin and/or a base pair such as uracil.
    83. 83. The system of any one of aspects 76 to 82, wherein the vessel also contains a surfactant.
    84. 84. The system of any one of aspects 76 to 83, wherein the vessel also contains a mineral.
    85. 85. The system of any one of aspects 76 to 84, wherein the vessel also contains a chelating agent.
    86. 86. The system of aspect 76 to 85, wherein the vessel has a total volume of greater than about 1,000 L, such as greater than 5,000 L.
    87. 87. The system of any one of aspects 75 to 86, comprising a radiation module and a sonication module.
    88. 88. The system of aspect 75, wherein the two or more modules comprise the radiation module and the sonication module, and wherein the biomass transportation subsystem is arranged to move biomass from the radiation module to the sonication module or vice versa, and from the preparation module to the pretreatment modules and vice versa.
    89. 89. The system of aspect 87 or aspect 88, further comprising the oxidation module.
    90. 90. The system of any one of aspects 75 to 89, further comprising a fermentation module.
    91. 91. The system of aspect 75, comprising the radiation module and the pyrolysis module.
    92. 92. The system of aspect 91, wherein the biomass transportation subsystem is arranged to move biomass from the radiation module to the pyrolysis module or vice versa.
    93. 93. The system of any one of aspects 91 to 93, further comprising the oxidation module.
    94. 94. The system of any of aspects 91 to 93, further comprising a fermentation module.
    95. 95. The system of any one of aspects 75 to 94, wherein a plurality of the two or more modules are implemented as parts of a single device.
    96. 96. The system of any one of aspects 75 to 95, wherein the two or more different pretreatment modules comprise radiation and sonication modules, radiation and oxidation modules, radiation and pyrolization modules, sonication and oxidation modules, sonication and pyrolization modules, or oxidation and pyrolization modules.
    97. 97. The system of aspect 96, further comprising a fermentation module.
    98. 98. The system of aspect 96, wherein the system comprises three or more different pretreatment modules.
    99. 99. The system of any one of aspects 96 to 98, wherein a plurality of the two or more modules are implemented as parts of a single device.
    100. 100. The system of any one of aspects 96 to 99, wherein the biomass transportation subsystem is arranged to move biomass between modules in any order.
    101. 101. The system of aspect 100, wherein the biomass transportation subsystem comprises a conveyor belt of fluidized bed.
    102. 102. The system of any one of aspects 75 to 101, wherein the radiation module is arranged to apply a dose of radiation of between about 10 MRads and about 100 MRads to the biomass, particularly between about 10 MRads and about 50 MRads, and more particularly between about 20 MRads and about 50 MRads.
    103. 103. The system of any one of aspects 75 to 102, wherein the radiation module is arranged to apply a dose of radiation sufficient to change the structure of the biomass, e.g., to reduce the average molecular weight of the biomass; to reduce the average crystallinity of the biomass; to increase the surface area of the biomass; to change the polymerization of the biomass, to increase the porosity of the biomass; and/or to change the chemical structure of the biomass.
    104. 104. The system of any one of aspects 75 to 103, wherein the sonication module is arranged to apply sonic energy at a frequency of between about 15 kHz and about 25 kHz.
    105. 105. The system of any of aspects 75 to 104, wherein the sonication module is arranged to apply sonic energy sufficient to change the structure of the biomass, e.g., to reduce the average molecular weight of the biomass; to reduce the average crystallinity of the biomass; to increase the surface area of the biomass; to change the polymerization of the biomass, to increase the porosity of the biomass; and/or to change the chemical structure of the biomass.
    106. 106. The system of any one of aspects 75 to 105, wherein the radiation module comprises radioactive material.
    107. 107. The system of any one of aspects 75 to 105, wherein the radiation module comprises an electron beam emitter.
    108. 108. A carbohydrate material produced by a process comprising pretreating a sheared biomass feedstock with any one or more of radiation, sonication, oxidation, pyrolysis and steam explosion.
    109. 109. The carbohydrate material of aspect 108, wherein pretreating is performed with any two or more of radiation, sonication, oxidation, pyrolysis, and steam explosion.
    110. 110. A carbohydrate material produced by a process comprising pretreating a biomass feedstock with any two or more of radiation, sonication, oxidation, pyrolysis, and steam explosion.
    111. 111. The carbohydrate of aspect 110, wherein pretreating is performed with any three or more of radiation, sonication, oxidation, pyrolysis, and steam explosion.
    112. 112. A composition comprising a cellulosic or a lignocellulosic material having a peak maximum molecular weight of less than about 25,000, and a crystallinity of less than about 55 percent.
    113. 113. The composition of aspect 112, wherein the cellulosic or a lignocellulosic material has a porosity of greater than about 72 percent.
    114. 114. The composition of aspect 112 or 113, wherein the cellulosic or lignocellulosic material has a BET surface greater than about 0.75 m2/g.
    115. 115. The composition of any one of aspects 112 to 114, wherein the cellulosic or lignocellulosic material has a bulk density of less than about 0.5 g/cm.
    116. 116. The composition of any one of aspects 112 to 115, wherein the cellulosic or lignocellulosic material comprises fibers having a length-to-diameter of greater than about 5.
    117. 117. The composition of any one of aspects 112 to 116, wherein the composition further comprises an enzyme and/or a microbe.
    118. 118. A composition comprising a cellulosic or a lignocellulosic material comprising fibers, wherein the cellulosic or lignocellulosic material has a peak maximum molecular weight of less than about 25,000, and a bulk density of less than about 0.5 g/cm3.
    119. 119. The composition of aspect 118, wherein the fibers have a length-to-diameter of greater than about 5.
    120. 120. A method of making a composite, such as a fiber-resin composite, the method comprising: irradiating a fibrous material comprising a first cellulosic and/or lignocellulosic material having a first molecular weight to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight; and combining the second cellulosic and/or lignocellulosic material with a material, such as a resin.
    121. 121. A method of making a composite, such as a fiber-resin composite, the method comprising: combining a material, such as a resin, with a fibrous material comprising a cellulosic and/or lignocellulosic material having a first molecular weight to provide a composite comprising the fibrous material and a matrix; and irradiating the composite to increase molecular weight of the first cellulosic and/or lignocellulosic material within the matrix, such as a resin matrix.
    122. 122. A method of making a composite, such as a fiber-resin composite, the method comprising: irradiating a fibrous material comprising a first cellulosic and/or lignocellulosic material having a first molecular weight to provide a second cellulosic and/or lignocellulosic material having a second molecular weight higher than the first molecular weight combining the second cellulosic and/or lignocellulosic material with a material, such as a resin, to provide a composite; and
      irradiating the composite.
    123. 123. A method of making an irradiated wood product, the method comprising providing a wood product comprising a first carbohydrate-containing material having a first molecular weight; and irradiating the wood product to provide an irradiated wood product comprising a second carbohydrate-containing material having a second molecular weight higher than the first molecular weight.
    124. 124. The method of any one of aspects 120 to 123, wherein the method further comprises sonicating, e.g., prior to, after, or concurrently with the irradiating.

Claims (15)

  1. A method comprising:
    irradiating a layer of lignocellulosic material with a series of doses of radiation, using more than one electron beam device, to deliver to the lignocellulosic material a total dose of radiation of at least 20 Mrad; and
    converting the irradiated material with an enzyme or microorganism to produce sugars.
  2. The method of claim 1 further comprising moving the lignocellulosic material through and between the electron beam devices.
  3. The method of claim 1 or 2 wherein the lignocellulosic material is selected from the group consisting of grasses, rice hulls, bagasse, jute, hemp, flax, bamboo, sisal, abaca, straw, corn cobs, corn stover, alfalfa, hay, coconut hair, seaweed, algae, and mixtures thereof.
  4. The method of claim 3 wherein the lignocellulosic material comprises corn cobs or corn stover.
  5. The method of any one of the above claims wherein irradiating is performed at a dose rate of 1 Mrad/s to 10 Mrad/s.
  6. The method of any one of the above claims wherein irradiating comprises applying to the material a total dose of between 20 MRads and 50 MRads.
  7. The method of any one of the above claims wherein at least one of the electron beam devices delivers electrons having an energy of 0.3 MeV to 2.0 MeV.
  8. The method of claim 7 wherein at least one of the electron beam devices delivers electrons having an energy of 0.7 MeV to 1.25 MeV.
  9. The method of any one of the above claims wherein converting comprises contacting the irradiated material with a cellulase in an aqueous medium.
  10. The method of any one of the above claims, the method further comprising comminuting the lignocellulosic material prior to irradiating.
  11. The method of claim 10 wherein comminuting the lignocellulosic material comprises subjecting the material to one or more of the following: stone grinding, mechanical ripping or tearing, pin grinding, milling, or air attrition milling.
  12. The method of claim 11 wherein comminuting comprises milling the material.
  13. The method of any one of the above claims further comprising fermenting the sugars to produce a combustible fuel.
  14. The method of claim 13 wherein the combustible fuel is selected from the group consisting of alcohols, organic acids, hydrocarbons, and mixtures thereof.
  15. The method of claim 14 wherein the combustible fuel comprises an alcohol, e.g., ethanol or butanol.
EP11007762A 2006-10-26 2007-10-26 Porcess of making sugars from biomass Ceased EP2415819A3 (en)

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US86329006P 2006-10-27 2006-10-27
US85991106P 2006-11-17 2006-11-17
US87514406P 2006-12-15 2006-12-15
US88189107P 2007-01-23 2007-01-23
EP07870818A EP2069423A2 (en) 2006-10-26 2007-10-26 Processing biomass

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Families Citing this family (311)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
TR200201034T2 (en) * 1999-10-15 2002-08-21 Cargill Incorporated Fibers made from plant seeds and their uses
US7692050B2 (en) 2003-03-28 2010-04-06 Ab-Cwt, Llc Apparatus and process for separation of organic materials from attached insoluble solids, and conversion into useful products
US8003833B2 (en) 2003-03-28 2011-08-23 Ab-Cwt, Llc Process for conversion of organic, waste, or low-value materials into useful products
US8877992B2 (en) 2003-03-28 2014-11-04 Ab-Cwt Llc Methods and apparatus for converting waste materials into fuels and other useful products
DE10323774A1 (en) * 2003-05-26 2004-12-16 Khd Humboldt Wedag Ag Process and plant for the thermal drying of a wet ground cement raw meal
US7669349B1 (en) * 2004-03-04 2010-03-02 TD*X Associates LP Method separating volatile components from feed material
US7024800B2 (en) * 2004-07-19 2006-04-11 Earthrenew, Inc. Process and system for drying and heat treating materials
US7987613B2 (en) * 2004-10-12 2011-08-02 Great River Energy Control system for particulate material drying apparatus and process
US9168469B2 (en) 2004-12-22 2015-10-27 Chemtor, Lp Method and system for production of a chemical commodity using a fiber conduit reactor
US10526299B2 (en) 2004-12-22 2020-01-07 Chemtor, Lp Fiber conduit reactor with a heat exchange medium inlet and a heat exchange medium outlet
US8128825B2 (en) 2004-12-22 2012-03-06 Chemtor, Lp Method and system for production of biofuels using a fiber conduit reactor
US9169597B2 (en) 2005-03-10 2015-10-27 Applied Cleantech Inc. Method of recycling fibers from sewage sludge and means thereof
AR057141A1 (en) 2005-09-28 2007-11-21 Cwt Llc Ab DEPOLIMERIZATION PROCESSING TO CONVERT ORGANIC AND NON-ORGANIC WASTE PRODUCTS IN USEFUL PRODUCTS
PL2007945T3 (en) * 2006-03-29 2011-06-30 Virginia Tech Intellectual Properties Inc Cellulose-solvent-based lignocellulose fractionation with modest reaction conditions and reagent cycling
US9499635B2 (en) 2006-10-13 2016-11-22 Sweetwater Energy, Inc. Integrated wood processing and sugar production
CA2823361C (en) 2006-10-26 2014-09-16 Xyleco, Inc. Methods of processing biomass comprising electron-beam radiation
US20100124583A1 (en) 2008-04-30 2010-05-20 Xyleco, Inc. Processing biomass
US7676953B2 (en) * 2006-12-29 2010-03-16 Signature Control Systems, Inc. Calibration and metering methods for wood kiln moisture measurement
KR100873700B1 (en) * 2007-06-25 2008-12-12 사단법인 한국가속기 및 플라즈마 연구협회 Method of producing bio-fuel using electron beam
US8617281B2 (en) 2007-08-13 2013-12-31 Applied Cleantech, Inc Methods and systems for feedstock production from sewage and product manufacturing therefrom
PT2254913T (en) * 2008-03-14 2017-10-23 Virginia Tech Intellectual Properties Inc Method for lignocellulose pretreatment using a super-cellulose-solvent and highly volatile solvents
GB2458529A (en) * 2008-03-25 2009-09-30 Saigas Ltd Extracting energy products from biomass using solar energy
JP4382856B2 (en) 2008-04-08 2009-12-16 株式会社谷黒組 Organic waste treatment method and thermal energy utilization method
NZ733050A (en) 2008-04-30 2019-01-25 Xyleco Inc Processing biomass with irradiation
US7931784B2 (en) 2008-04-30 2011-04-26 Xyleco, Inc. Processing biomass and petroleum containing materials
US8236535B2 (en) 2008-04-30 2012-08-07 Xyleco, Inc. Processing biomass
US7867358B2 (en) 2008-04-30 2011-01-11 Xyleco, Inc. Paper products and methods and systems for manufacturing such products
US20090312537A1 (en) * 2008-04-30 2009-12-17 Xyleco, Inc. Carbohydrates
US8212087B2 (en) 2008-04-30 2012-07-03 Xyleco, Inc. Processing biomass
CN102084058B (en) * 2008-05-21 2014-10-22 应用清洁技术公司 Methods and systems for feedstock production from sewage and product manufacturing therefrom
WO2009155337A2 (en) 2008-06-18 2009-12-23 Xyleco, Inc. Processing materials with ion beams
US8168840B2 (en) 2008-06-25 2012-05-01 Kior Inc. Biomass pretreatment process
US7900857B2 (en) 2008-07-17 2011-03-08 Xyleco, Inc. Cooling and processing materials
CN101333447B (en) * 2008-08-07 2012-03-21 上海交通大学 Process for preparing bio-oil by co-pyrolyzing marine algae and land biomass
KR101270561B1 (en) * 2008-08-08 2013-06-03 가오 가부시키가이샤 Biodegradable resin composition
US8618325B2 (en) 2008-08-12 2013-12-31 4A Technologies, Llc Modularized system and method for urea production using a bio-mass feedstock
US9352329B2 (en) 2008-08-12 2016-05-31 4A Technologies, Llc Modularized system and method for urea production using a bio-mass feedstock
US8103385B2 (en) * 2008-09-30 2012-01-24 Rockwell Automation Technologies, Inc. Optimizing product drying through parallel lines of centrifuges and dryer process units
US7984567B2 (en) * 2008-10-07 2011-07-26 Christ Bill Bertakis Apparatus for cleaning simulated hair articles
KR101689797B1 (en) * 2008-10-28 2016-12-26 질레코 인코포레이티드 Processing materials
EA027923B1 (en) * 2008-11-17 2017-09-29 Ксилеко, Инк. Processing biomass
AU2014271224B2 (en) * 2008-11-17 2017-05-25 Xyleco, Inc. Processing biomass
FR2939446B1 (en) * 2008-12-05 2011-04-22 Valagro Carbone Renouvelable USE OF RECYCLED COTTON FOR PRODUCING ETHANOL, AND PROCESS FOR PRODUCING THE SAME.
CA2781862C (en) * 2008-12-09 2018-02-13 Sweetwater Energy, Inc. Ensiling biomass for biofuels production and multiple phase apparatus for hydrolyzation of ensiled biomass
US8552233B2 (en) 2008-12-16 2013-10-08 Kior Inc. Pretreatment of biomass with carbonaceous material
BRPI0923020A2 (en) * 2008-12-19 2015-12-15 Xyleco Inc recalcitrance reduction method in cellulosic or lignocellulosic materials and composition.
DK2367974T3 (en) * 2008-12-23 2018-03-05 Inaeris Tech Llc Modification of biomass for efficient fuel conversion
RU2405832C2 (en) 2008-12-29 2010-12-10 Дэвон Инвестмент Лимитед Method of preparing wood raw material to obtain sugars, installation for realising said method and product
CA2738886C (en) * 2009-01-16 2012-02-21 Greenfield Ethanol Inc. Removal of inhibitory compounds during pre-treatment of lignocellulosic biomass
AU2013203130B2 (en) * 2009-01-26 2014-12-18 Xyleco, Inc. Processing biomass
EA201790375A1 (en) * 2009-01-26 2018-01-31 Ксилеко, Инк. BIOMASS PROCESSING
AU2016222347B2 (en) * 2009-02-11 2018-09-20 Xyleco, Inc. Saccharifying biomass
SG2014007140A (en) * 2009-02-11 2014-05-29 Xyleco Inc Processing biomass
US20100203607A1 (en) 2009-02-11 2010-08-12 Xyleco, Inc. Processing biomass
AP4009A (en) 2009-02-11 2017-01-19 Xyleco Inc Saccharifying biomass
KR101569013B1 (en) * 2009-02-16 2015-11-16 삼성전자주식회사 Method for Pretreating and Saccharifying Marine Algae Biomass
US20100223804A1 (en) * 2009-02-27 2010-09-09 Flaherty John R Air modulating non-thermal dryer
US8558043B2 (en) * 2009-03-04 2013-10-15 Kior, Inc. Modular biomass treatment unit
US20110111456A1 (en) 2009-04-03 2011-05-12 Xyleco, Inc. Processing biomass
KR101037125B1 (en) 2009-05-14 2011-05-26 계명대학교 산학협력단 Biomass Pretreatment Method for Preparing Bioethanol
AU2010249679B2 (en) * 2009-05-20 2015-02-05 Xyleco, Inc. Processing biomass
UA113872C2 (en) * 2009-05-20 2017-03-27 Bioprocessing
KR101735543B1 (en) * 2009-05-20 2017-05-15 질레코 인코포레이티드 Processing biomass
BRPI1012256A2 (en) * 2009-06-23 2019-04-16 American Process Inc biorefinery process and process for enzymatic hydrolysis of cellulose fiber
RU2507330C2 (en) * 2009-07-13 2014-02-20 БЕТА РЕНЬЮЭБЛС С.п.А. High-temperature method of separating lignin
US8772406B2 (en) * 2009-08-06 2014-07-08 Robert J. Linhardt Synthetic wood composite
ES2458554T3 (en) 2009-08-24 2014-05-06 Abengoa Bioenergy New Technologies, Inc. Procedures for the production of ethanol and co-products from cellulosic biomass
CH701959B1 (en) * 2009-10-01 2012-04-30 Kremlin Group Corp Cellulosic mass.
WO2011041756A2 (en) * 2009-10-01 2011-04-07 Mississippi State University Method of increasing anhydrosugars, pyroligneous fractions and esterified bio-oil
BRPI1002758A2 (en) * 2009-10-06 2012-10-30 Kl Energy Corp process for thermomechanical biomass pretreatment and biomass pretreatment combiner
JP4538595B1 (en) * 2009-10-07 2010-09-08 克守 谷黒 Biomass material processing method and thermal energy utilization method
AU2015243068B2 (en) * 2009-10-14 2017-06-01 Xyleco, Inc. Producing edible residues from ethanol production
ES2671798T3 (en) 2009-10-14 2018-06-08 Xyleco, Inc. Edible waste production from ethanol production
LT2488918T (en) 2009-10-14 2018-09-10 Xyleco, Inc. Marking paper products
JP5108853B2 (en) * 2009-10-16 2012-12-26 浦安電設株式会社 Wet organic waste treatment system
ES2854723T3 (en) * 2009-11-25 2021-09-22 Anitox Corp Carbohydrate fermentation
PT2509916E (en) * 2009-12-09 2014-04-02 Ingeborg Klose Method for producing phosphates and compounds containing phosphates, in particular alkaline-earth phosphates, alkaline-earth silicophosphates or alkaline-earth oxides
AU2011205510B2 (en) * 2010-01-15 2014-09-11 Xyleco, Inc. Cooling and processing materials
US8691526B2 (en) 2010-01-20 2014-04-08 Xyleco, Inc. Processing materials
NZ717649A (en) 2010-01-20 2017-07-28 Xyleco Inc Method and system for saccharifying and fermenting a biomass feedstock
MY175991A (en) 2010-01-20 2020-07-20 Xyleco Inc Dispersing feedstocks and processing materials
SG10201501234XA (en) * 2010-02-17 2015-04-29 Xyleco Inc Processing biomass
RU2607632C2 (en) * 2010-02-19 2017-01-10 Энерпи Б.В. Wastes photonic radiolysis
JP2011182646A (en) * 2010-03-04 2011-09-22 Hamamatsu Photonics Kk Method for treating lignocellulose-based biomass
JP2011225658A (en) * 2010-04-16 2011-11-10 Sumitomo Electric Ind Ltd Method for pretreatment of biomass
EA201790127A3 (en) 2010-05-24 2017-09-29 Ксилеко, Инк. BIOMASS PROCESSING
AU2011258568B2 (en) * 2010-05-24 2015-11-26 Xyleco, Inc. Processing chemicals
WO2011159949A2 (en) * 2010-06-16 2011-12-22 Applied Chemical Laboratories, Inc. Degradation of biomass by metal-catalzyed peroxide oxidation
US20100323435A1 (en) * 2010-06-25 2010-12-23 Boateng Akwasi A Injection System for Bio-fuel Reactor
WO2012002483A1 (en) * 2010-06-30 2012-01-05 マイクロ波環境化学株式会社 Oily substance production process, and oily substance production device
US20130230624A1 (en) * 2010-07-01 2013-09-05 Commonwealth Scientific And Industrial Research Organisation Treatment of plant biomass
JP5713591B2 (en) * 2010-07-05 2015-05-07 本田技研工業株式会社 Saccharification pretreatment equipment for lignocellulosic biomass
JP5779323B2 (en) * 2010-07-05 2015-09-16 本田技研工業株式会社 Pre-saccharification method for lignocellulosic biomass
FI126855B (en) * 2010-07-08 2017-06-30 Aalto-Korkeakoulusäätiö Process and apparatus for producing organic solvents and alcohols with microbes
BR112013001307A2 (en) * 2010-07-19 2017-06-20 Xyleco Inc biomass processing
CN101906325B (en) * 2010-07-20 2013-09-04 阳光凯迪新能源集团有限公司 Process and apparatus thereof for low-temperature cracking and high-temperature gasification of biomass
NL1038175C2 (en) * 2010-08-19 2012-02-21 Danvos B V A process for the conversion of biomass of plant origen, and a combustion process.
RU2545576C2 (en) * 2010-09-29 2015-04-10 БЕТА РЕНЬЮЭБЛС С.п.А. Biomass, subjected to preliminary processing, characterised by improved fermentative availability
AU2015203341B2 (en) * 2010-10-20 2017-03-30 Xyleco, Inc. Method For Treating Lignocellulosic Material By Irradiating With An Electron Beam
MY159993A (en) * 2010-10-20 2017-02-15 Xyleco Inc Method for treating lignocellulosic material by irradiating with an electron beam
CN101979641B (en) * 2010-10-20 2012-10-03 湖南农业大学 Method for refining sugar by rapidly degrading reed fibers
US9243078B2 (en) * 2010-11-23 2016-01-26 Ecohelix Ab Method to increase the molecular weight of wood mannans and xylans comprising aromatic moieties
WO2012080702A2 (en) * 2010-12-15 2012-06-21 Imperial Innovations Ltd Treatment
AU2011349318B2 (en) * 2010-12-20 2015-08-20 Shell International Research Maatschappij B.V. Process to produce biofuels from biomass
CN102174595A (en) * 2011-02-01 2011-09-07 中国科学院过程工程研究所 Method for producing butanol by continuous solid state fermentation of restaurant-kitchen garbage
DE102011010193A1 (en) * 2011-02-02 2012-08-02 Biowert Ag Fiber reinforced plastic material
JP5951181B2 (en) * 2011-02-07 2016-07-13 株式会社北川鉄工所 Method for saccharification of lignocellulosic biomass
KR20130140114A (en) * 2011-02-14 2013-12-23 질레코 인코포레이티드 Processing biomass
CN103328640A (en) 2011-02-14 2013-09-25 希乐克公司 Processing paper stock
WO2013106025A1 (en) * 2011-04-07 2013-07-18 Renewable Oil International, LLC Method and apparatus for a combination moving bed thermal treatment reactor and moving bed filter
EP3786262A1 (en) 2011-04-15 2021-03-03 Carbon Technology Holdings, LLC Processes for producing high-carbon biogenic reagents
US20130149765A1 (en) * 2011-05-11 2013-06-13 Gary N. Austin Anaerobic digester for the production of methane gas from organic waste
FI126965B (en) * 2011-05-18 2017-08-31 Fortum Oyj Method and equipment for generating energy by recycling materials during the fuel combustion process
AP2016009603A0 (en) 2011-06-09 2016-12-31 Xyleco Inc Processing biomass
WO2013001629A1 (en) 2011-06-29 2013-01-03 マイクロ波環境化学株式会社 Chemical reaction apparatus, and chemical reaction method
CN102860412A (en) * 2011-07-06 2013-01-09 吉林大学 Co-production method for distilled spirit and livestock total nutrient feed through alfalfa fermentation
US8329455B2 (en) 2011-07-08 2012-12-11 Aikan North America, Inc. Systems and methods for digestion of solid waste
JP5798821B2 (en) * 2011-07-15 2015-10-21 三菱重工業株式会社 Method and system for producing gasoline from methanol and generating electricity
WO2013010271A1 (en) 2011-07-15 2013-01-24 Greenfield Ethanol Inc. Conditioning of biomass for improved c5/c6 sugar release prior to fermentation
KR101316733B1 (en) * 2011-09-23 2013-10-10 한국과학기술연구원 Method for manufacturing detoxificated lignocellulosic biomass hydrolysate with decreased or eliminated toxicity and method for manufacturing organic or and biofuel using the same
AU2013201308B2 (en) * 2011-10-13 2015-01-29 Alebund Pharmaceuticals (Hong Kong) Limited Iron-fiber composition, preparation and uses thereof
US11279964B2 (en) * 2011-10-25 2022-03-22 Purac Biochem B.V. Process for the conversion of lignocellulose material into an organic acid
US9550943B2 (en) * 2011-10-27 2017-01-24 Raymond Roger Wallage Efficient oil shale recovery method
EP2776536A1 (en) * 2011-11-09 2014-09-17 Vertichem Corporation A method for producing biobased chemicals from plant biomass
JP5109004B1 (en) 2011-11-11 2012-12-26 マイクロ波化学株式会社 Chemical reactor
US11229895B2 (en) 2011-11-11 2022-01-25 Microwave Chemical Co., Ltd. Chemical reaction method using chemical reaction apparatus
US9856606B2 (en) 2011-12-12 2018-01-02 Enzymatic Deinking Technologies, L.L.C. Enzymatic pre-treatment of market pulp to improve fiber drainage and physical properties
US8940060B2 (en) 2011-12-15 2015-01-27 Uop Llc Methods and apparatuses for forming low-metal biomass-derived pyrolysis oil
CN104011219A (en) 2011-12-22 2014-08-27 希乐克公司 Processing biomass
MY169799A (en) 2011-12-22 2019-05-16 Xyleco Inc Processing biomass for use in fuel cells related applications
CN104039972A (en) * 2011-12-22 2014-09-10 希乐克公司 Processing of biomass material
UA117450C2 (en) 2011-12-22 2018-08-10 Ксілеко, Інк. Processing biomass for use in fuel cells
US8765430B2 (en) 2012-02-10 2014-07-01 Sweetwater Energy, Inc. Enhancing fermentation of starch- and sugar-based feedstocks
JP5987223B2 (en) * 2012-03-06 2016-09-07 愛媛県 Method for producing cellulose solution, method for producing cellulose, method for saccharification of cellulose
US20150018584A1 (en) * 2012-04-13 2015-01-15 Sweetwater Energy, Inc. Methods and Systems for Saccharification of Biomass
US8563277B1 (en) * 2012-04-13 2013-10-22 Sweetwater Energy, Inc. Methods and systems for saccharification of biomass
RU2488445C1 (en) * 2012-04-26 2013-07-27 Общество с ограниченной ответственностью "Целлокорм" Synthesis of multifunctional catalyst for oxidative cracking of organic material and method for liquid-phase low-temperature oxidative cracking of organic material (versions)
SI2847127T1 (en) 2012-05-07 2021-01-29 Carbon Technology Holdings, LLC Continuous process for producing biogenic activated carbon
DK2860269T3 (en) * 2012-05-18 2017-09-11 Toray Industries Process for preparing a sugar solution
US8464437B1 (en) * 2012-05-25 2013-06-18 Wyssmont Company Inc. Apparatus and method for the treatment of biosolids
US9752164B2 (en) * 2012-06-15 2017-09-05 Microvi Biotech, Inc. Enhanced efficiency ethanol and sugar conversion processes
US9334507B2 (en) 2012-06-15 2016-05-10 Microvi Biotech, Inc. Bioprocesses for making butanol
US20140178944A1 (en) * 2012-06-29 2014-06-26 Sweetwater Energy, Inc. Preservation of Biomass for Pretreatment
UA116630C2 (en) 2012-07-03 2018-04-25 Ксілеко, Інк. METHOD OF CONVERTING SUGAR TO FURFURYL ALCOHOL
WO2014047195A1 (en) 2012-09-18 2014-03-27 Chemtor, Lp Use of a fiber conduit contactor for metal and/or metalloid extraction
MX2015003337A (en) * 2012-09-18 2015-08-12 Proton Power Inc C-o-h compound processing for hydrogen or liquid fuel production.
NZ747168A (en) 2012-10-10 2019-12-20 Xyleco Inc Treating biomass
US10689196B2 (en) 2012-10-10 2020-06-23 Xyleco, Inc. Processing materials
NZ706069A (en) * 2012-10-10 2018-11-30 Xyleco Inc Processing biomass
US9249080B2 (en) * 2012-10-17 2016-02-02 Anellotech, Inc. Chemical intermediates by catalytic fast pyrolysis process
WO2014066661A1 (en) * 2012-10-25 2014-05-01 Queston, Inc. Clean burning wood biomass fuel and method of producing same
WO2014087949A1 (en) * 2012-12-05 2014-06-12 宇部興産株式会社 Biomass solid fuel
KR101493227B1 (en) * 2012-12-12 2015-03-02 한국세라믹기술원 Pretreatment method of lignocellulose biomass, and manufacturing method of saccharides and biofuel using the same
US9410258B2 (en) 2012-12-21 2016-08-09 Colorado Energy Research Technologies, LLC Systems and methods of improved fermentation
US9279101B2 (en) 2012-12-21 2016-03-08 Colorado Energy Research Technologies, LLC Systems and methods of improved fermentation
US9365525B2 (en) 2013-02-11 2016-06-14 American Science And Technology Corporation System and method for extraction of chemicals from lignocellulosic materials
NZ706072A (en) 2013-03-08 2018-12-21 Xyleco Inc Equipment protecting enclosures
CN108893251A (en) * 2013-03-08 2018-11-27 希乐克公司 Reconfigurable tooling housing
CN105007759B (en) 2013-03-08 2018-11-20 上海礼邦医药科技有限公司 Metal ion-functional fiber component complex compositions, its preparation and purposes
WO2014145689A1 (en) * 2013-03-15 2014-09-18 All Power Labs, Inc. Simultaneous pyrolysis and communition for fuel flexible gasification and pyrolysis
US9850512B2 (en) 2013-03-15 2017-12-26 The Research Foundation For The State University Of New York Hydrolysis of cellulosic fines in primary clarified sludge of paper mills and the addition of a surfactant to increase the yield
US9453170B2 (en) 2013-03-15 2016-09-27 All Power Labs, Inc. Hybrid fixed-kinetic bed gasifier for fuel flexible gasification
US11118308B2 (en) 2013-03-15 2021-09-14 Ip2Ipo Innovations Limited Treatment of lignocellulosic biomass with ionic liquid
US9809867B2 (en) 2013-03-15 2017-11-07 Sweetwater Energy, Inc. Carbon purification of concentrated sugar streams derived from pretreated biomass
KR101458981B1 (en) * 2013-04-04 2014-11-10 한국과학기술연구원 Electrochemical detoxification of lignocellulosic hydrolysates for biochemical or biofuel production and detoxificated lignocellulosic hydrolysates
JP2016516870A (en) 2013-04-26 2016-06-09 ザイレコ,インコーポレイテッド Processing of hydroxy-carboxylic acids into polymers
WO2014176508A2 (en) 2013-04-26 2014-10-30 Xyleco, Inc. Processing biomass to obtain hydroxylcarboxylic acids
KR101658424B1 (en) * 2013-04-30 2016-09-22 충남대학교산학협력단 The method of manufacturing cellulose and method of manufacturing a cellulose-based polymer having antimicrobial
BR112015026769B1 (en) * 2013-05-17 2020-01-07 Xyleco, Inc. METHOD TO PRODUCE ASPARTIC ACID
WO2014186652A1 (en) * 2013-05-17 2014-11-20 Xyleco, Inc. Processing biomass
CN105452472B (en) 2013-06-12 2020-03-13 雷内科学有限公司 Method for treating Municipal Solid Waste (MSW) by microbial hydrolysis and fermentation
RU2535967C1 (en) * 2013-09-02 2014-12-20 Общество с ограниченной ответственностью "Научная интеграция" Method of preparation of raw material for anaerobic processing of organic wastes and the unit for its implementation
WO2015035077A1 (en) * 2013-09-04 2015-03-12 Foster Agblevor Catalytic pyrolysis of olive mill waste
WO2015061701A1 (en) 2013-10-24 2015-04-30 Biogenic Reagent Ventures, Llc Methods and apparatus for producing activated carbon from biomass through carbonized ash intermediates
US20150147786A1 (en) * 2013-11-24 2015-05-28 E I Du Pont De Nemours And Company High force and high stress destructuring for starch biomass processing
DE102013114386A1 (en) * 2013-12-18 2015-06-18 Uwe D'Agnone Process for the preparation of grass for the production of paper, cardboard and cardboard
US9475031B2 (en) 2014-01-16 2016-10-25 Biogenic Reagents Ventures, Llc Carbon micro-plant
CA2977092C (en) 2014-02-24 2022-12-13 Biogenic Reagents Ventures, Llc Highly mesoporous activated carbon
US9951363B2 (en) 2014-03-14 2018-04-24 The Research Foundation for the State University of New York College of Environmental Science and Forestry Enzymatic hydrolysis of old corrugated cardboard (OCC) fines from recycled linerboard mill waste rejects
WO2015142541A1 (en) 2014-03-21 2015-09-24 Xyleco, Inc. Method and structures for processing materials
JP2015183095A (en) * 2014-03-24 2015-10-22 凸版印刷株式会社 Functional cellulose, manufacturing method thereof and functional cellulose dispersion and molding
US10195562B2 (en) * 2014-04-09 2019-02-05 Empire Technology Development Llc Apparatuses, methods, and systems for removal of target compounds from gases
CN103981751B (en) * 2014-05-09 2016-04-20 中国农业大学 A kind of with section wood useless after cultivation of glossy ganoderma for raw material extracts cellulosic method
CN103980929B (en) * 2014-05-20 2015-06-24 北京林业大学 Method for preparing biological fuel oil by fast pyrolyzing biomass
WO2015183034A1 (en) * 2014-05-30 2015-12-03 한국화학연구원 Metal nanoparticles, and preparation method therefor
JP6405751B2 (en) * 2014-07-01 2018-10-17 凸版印刷株式会社 Method for producing fine cellulose
US20170152468A1 (en) * 2014-07-03 2017-06-01 Renature, Inc. Biodigestion reactor, system including the reactor, and methods of using same
CU20170058A7 (en) 2014-07-08 2018-02-08 Xyleco Inc METHOD FOR MARKING A PLASTIC-BASED PRODUCT THROUGH ION IMPLEMENTATION
US9382283B2 (en) 2014-08-01 2016-07-05 American Science And Technology Corporation Oxygen assisted organosolv process, system and method for delignification of lignocellulosic materials and lignin recovery
CN104294693B (en) * 2014-08-15 2016-08-17 施波波 A kind of preparation method of micro-nano cellulose
TWI571608B (en) * 2014-08-15 2017-02-21 行政院原子能委員會核能研究所 Waste heat recovery apparatus and method thereof
KR20160022191A (en) 2014-08-19 2016-02-29 한국에너지기술연구원 Hyophobic coal-biomass granule type mixed fuel, apparatus and manufacturing method thereof using biomass ethanol process
DE102014013777A1 (en) * 2014-09-17 2016-03-17 Maria Rogmans Method for operating a biogas plant
MX2017003594A (en) 2014-09-19 2017-05-12 Xyleco Inc Saccharides and saccharide compositions and mixtures.
US11390822B2 (en) 2014-10-07 2022-07-19 Ube Industries, Ltd. Biomass solid fuel
WO2016065357A1 (en) 2014-10-24 2016-04-28 Biogenic Reagent Ventures, Llc Halogenated activated carbon compositions and methods of making and using same
GB201420770D0 (en) * 2014-11-21 2015-01-07 Bpb United Kingdom Ltd Fire resistant calcium sulphate-based products
HRP20221024T1 (en) 2014-12-09 2022-11-11 Sweetwater Energy, Inc. Rapid pretreatment
FR3030536B1 (en) * 2014-12-22 2018-06-15 Institut National Des Sciences Appliquees Lyon ORGANOPOLYSILOXANES AND PROCESS FOR THEIR PREPARATION
KR20160081027A (en) 2014-12-30 2016-07-08 한국에너지기술연구원 Hydrophobic surfaces coal mixed fuel containing lignin and manufacturing method thereof
CN105798320B (en) * 2014-12-31 2018-05-04 中国科学院化学研究所 A kind of method of low temperature preparation copper nanoparticle
CN104672298A (en) * 2015-03-11 2015-06-03 利穗科技(苏州)有限公司 Explosion-proof type protein chromatography system
CN104652156B (en) * 2015-03-20 2017-01-18 山东福田药业有限公司 Method for preparation of lignosulfonate and cogeneration of microcrystalline cellulose from corn cob residues
CA2980019C (en) * 2015-04-03 2023-09-12 Poet Research, Inc. Methods of compressing lignocellulosic feedstock into discrete units, and related systems
US10338184B2 (en) 2015-04-07 2019-07-02 Xyleco, Inc. Monitoring methods and systems for processing biomass
CN104862343A (en) * 2015-04-19 2015-08-26 北京化工大学 Lignocellulose simultaneous saccharification and fermentation method for predation of fuel ethanol
US10828801B2 (en) 2015-06-04 2020-11-10 Ra Energy Corporation Advanced microfibers and related methods
KR101695702B1 (en) 2015-07-09 2017-01-23 한국에너지기술연구원 MODIFICATION METHOD FOR LOW RANK COAL USING 2nd GENERATION BIOMASS COMPRISED OF HEXOSE
KR101709328B1 (en) 2015-07-09 2017-03-08 한국에너지기술연구원 MODIFICATION METHOD FOR LOW RANK COAL USING 2nd GENERATION BIOMASS COMPRISED OF PENTOSE
WO2017015242A1 (en) 2015-07-17 2017-01-26 The Regents Of The University Of California Conversion of a soiled post-consumer cellulosic composition
CN106480472B (en) * 2015-08-25 2019-03-12 中国科学院天津工业生物技术研究所 Convert one step of biological material to method, container and the purposes of solable matter
AU2015408175B2 (en) 2015-08-31 2021-08-05 Kimberly-Clark Worldwide, Inc. Improving the purity of materials recycled from disposable absorbent articles
US10384982B2 (en) * 2015-09-09 2019-08-20 Planet Found Energy Development, LLC Waste material processing system
GB201517882D0 (en) * 2015-10-09 2015-11-25 Knauf Insulation Ltd Wood particle boards
JP2018533660A (en) * 2015-11-12 2018-11-15 ザ リサーチ ファウンデーション フォー ザ ステイト ユニバーシティー オブ ニューヨーク Formation of carboxylated nanocellulose
US10894838B2 (en) 2015-11-12 2021-01-19 The Research Foundation For The State University Of New York Production of carboxylated nanocelluloses
GB201520453D0 (en) 2015-11-20 2016-01-06 Imp Innovations Ltd Process
EP3173201A1 (en) * 2015-11-30 2017-05-31 Omya International AG Calcium carbonate for particle boards
GB2546243B (en) 2015-12-23 2018-07-11 Aerothermal Green Energy Ltd Biomass, thermal pressure hydrolysis and anaerobic digestion
CN105713050B (en) * 2016-01-21 2018-12-25 河南农业大学 A kind of method that degradation selectivity corncob hemicellulose improves xylose yield
CN105542827B (en) * 2016-01-29 2017-10-20 华南理工大学 The biomass bio oil preparation system and method for a kind of ultrasonic wave ethanol-water system
JP6816372B2 (en) * 2016-03-25 2021-01-20 三菱ケミカル株式会社 How to recover ethanol
KR101945186B1 (en) 2016-04-05 2019-04-17 한국에너지기술연구원 De-mineralized Biomass, Manufacturing Method and System of Multi-fuel Production thereof
CA3019888A1 (en) 2016-04-06 2017-10-12 Ube Industries, Ltd. Biomass solid fuel
WO2017218756A1 (en) * 2016-06-17 2017-12-21 Armstrong World Industries, Inc. Pelletization of recycled ceiling materials
RU2637550C2 (en) * 2016-07-13 2017-12-05 Общество с ограниченной ответственностью "Малое инновационное предприятие "Югра-Биотехнологии" Method for production of composite materials
CN106239691A (en) * 2016-08-02 2016-12-21 浙江长兴森大竹木制品有限公司 A kind of low formaldehyde high-strength bamboo wood laminated particle-board
CN106217541A (en) * 2016-08-02 2016-12-14 南京博俊新材料有限公司 Liquid is optimized based on catalyst compounded furfuryl alcohol resin used for wood modification
CN106217540A (en) * 2016-08-02 2016-12-14 南京博俊新材料有限公司 Furfuryl alcohol resin for Wooden modifying optimizes liquid
CN106217576A (en) * 2016-08-02 2016-12-14 浙江长兴森大竹木制品有限公司 A kind of Masson Pine Mianzhu laminated particle-board
CN106155146A (en) * 2016-08-19 2016-11-23 上海德瑾绿水科技有限公司 The monitoring system of a kind of rubbish complete biodegradable mixing machine special and method thereof
CN106543768B (en) * 2016-09-27 2019-01-22 济南米铎碳新能源科技有限公司 The method for extracting stalk pigment using steam explosion technology
JP6858589B2 (en) * 2016-09-29 2021-04-14 太平洋セメント株式会社 Carbon-containing waste treatment method
CA2946264A1 (en) * 2016-10-25 2018-04-25 Nova Chemicals Corporation Use of semipermeable membranes in cracking coils
CN106671227A (en) * 2016-12-28 2017-05-17 汪四青 Treatment method for phoenix tree bark picture material
CA3053773A1 (en) 2017-02-16 2018-08-23 Sweetwater Energy, Inc. High pressure zone formation for pretreatment
CA3053898A1 (en) 2017-02-17 2018-08-23 The Research Foundation For The State University Of New York High-flux thin-film nanocomposite reverse osmosis membrane for desalination
JP2020516497A (en) * 2017-04-10 2020-06-11 ユニバーシティー オブ メリーランド,カレッジ パーク Strong and durable structural wood, and method of making and using the same
CN108729284A (en) * 2017-04-18 2018-11-02 兰州理工大学 A kind of ultrasonic pretreatment plant fiber device
US10645950B2 (en) 2017-05-01 2020-05-12 Usarium Inc. Methods of manufacturing products from material comprising oilcake, compositions produced from materials comprising processed oilcake, and systems for processing oilcake
CN107083253B (en) * 2017-05-12 2019-04-02 江苏大学 A kind of equipment and method of agriculture and forestry organic waste material and the total catalytic pyrolysis liquefaction of seaweed segmentation
TWI652290B (en) * 2017-08-01 2019-03-01 賴至慶 Preparation method and product of purified lignin composite material
KR101965841B1 (en) * 2017-09-05 2019-04-04 한국화학연구원 Method for pretreatment of biomass
CN107457976A (en) * 2017-09-21 2017-12-12 德清新亚塑业有限公司 A kind of PVC transparent box plastic uptake processing unit (plant)
CN107474261A (en) * 2017-09-25 2017-12-15 南京工业大学 A kind of method that biomass lignin is extracted using quaternary ammonium base
EP3461801B1 (en) * 2017-09-29 2021-10-27 Daw Se Method for the preparation of plant fibre insulation materials for injected or poured in insulation
WO2019084518A1 (en) 2017-10-27 2019-05-02 Xyleco, Inc. Processing biomass
KR102028451B1 (en) 2017-11-02 2019-11-14 한국에너지기술연구원 System for high concentration bio-liquid using 2nd generation biomass
CN108166293B (en) * 2017-12-04 2019-08-02 湖南省农业科学院 A kind of method and its system of irradiation-plant fibrous agricultural wastes of chemical method Combined Treatment
CN108580505A (en) * 2017-12-28 2018-09-28 宁波宝力农环境技术开发有限公司 Organic solid waste zero-emission and process for reclaiming
CN108118400A (en) * 2018-02-01 2018-06-05 德清县利通绢纺塑化有限公司 A kind of thin,tough silk bourette silk weaving spinning-drawing machine waste material collection device
EP3527643B1 (en) * 2018-02-16 2022-04-06 Università degli studi di Bergamo A method for carrying out pyrolysis of prime materials, particularly of prime materials deriving from tires or bitumen and a plant for carrying out pyrolysis operating according to the said method
PL239323B1 (en) * 2018-02-21 2021-11-22 Laszko Miroslaw Method for removing impurities from vapours expelled from paper-making machines
PL239324B1 (en) * 2018-02-21 2021-11-22 Laszko Miroslaw Method for recovery of water from vapours removed from the papermaking machine drying plant
CN108419919A (en) * 2018-03-19 2018-08-21 上海同化新材料科技有限公司 Functional feedstuff additive
KR101931785B1 (en) * 2018-03-19 2019-04-05 주식회사 코리아진텍 Manufacturing method of coal additive
US11534746B2 (en) 2018-04-06 2022-12-27 Utah State University Red mud compositions and methods related thereto
KR102134409B1 (en) 2018-05-28 2020-07-16 씨제이제일제당 주식회사 A physically pretreated biomass composition comprising a high concentration of biomass
KR102073898B1 (en) 2018-05-28 2020-02-05 씨제이제일제당 주식회사 A physically pretreated biomass composition capable of membrane filtration
US11638331B2 (en) 2018-05-29 2023-04-25 Kontak LLC Multi-frequency controllers for inductive heating and associated systems and methods
US11555473B2 (en) 2018-05-29 2023-01-17 Kontak LLC Dual bladder fuel tank
CN108865312B (en) * 2018-06-30 2020-11-27 嘉兴量创科技有限公司 Biofuel preparation facilities
CN108927187A (en) * 2018-07-03 2018-12-04 安徽圣宝新能源科技有限公司 A method of liquid fuel catalysing material is prepared rich in lignin stalk fermentation
EP3861057A1 (en) * 2018-10-05 2021-08-11 ROCKWOOL International A/S Method for producing oxidized lignins
US11261315B1 (en) * 2019-01-09 2022-03-01 North Carolina Agricultural And Technical State University Environmentally friendly asphalt binder additive
US10843952B2 (en) * 2019-02-25 2020-11-24 Avi Kagan Continuous, approximately real-time residential wastewater treatment system and apparatus
CN110273310A (en) * 2019-03-20 2019-09-24 杭州电子科技大学 A method of office waste is handled using MFC
CN110126036A (en) * 2019-04-19 2019-08-16 中国科学院理化技术研究所 A kind of rodlike stalk micron particles and preparation method thereof
CN110056860A (en) * 2019-04-25 2019-07-26 梅丽中 One kind shedding type biological particles from fragmentation
FR3097553B1 (en) 2019-06-24 2021-11-26 Europeenne De Biomasse PROCESS FOR THE PRODUCTION OF SOLID FUELS FROM END-OF-LIFE WOOD OR WOOD-WASTE
US11639010B2 (en) 2019-07-08 2023-05-02 Fermi Research Alliance, Llc Electron beam treatment for invasive pests
CN110982570B (en) * 2019-11-01 2021-06-08 安徽鑫邦生物质资源科技有限公司 Preparation method of biomass granular fuel with moisture-proof and high-heat-value functions
CN110815437B (en) * 2019-11-16 2022-03-01 湖南省波恩贝竹木科技有限公司 Bamboo furniture panel and preparation method thereof
CN110938448B (en) * 2019-12-03 2020-10-09 新奥生物质能(天津)有限公司 Control method and device of biomass pyrolysis device
CN111139116A (en) * 2019-12-05 2020-05-12 西安圣华农业科技股份有限公司 Method for preparing biomass fuel from straws
US11692000B2 (en) 2019-12-22 2023-07-04 Apalta Patents OÜ Methods of making specialized lignin and lignin products from biomass
KR102535324B1 (en) * 2020-01-29 2023-05-22 박기원 Freeze-dried Feed for Companion Animal and Method
US11690332B2 (en) 2020-04-03 2023-07-04 Rockwool A/S Method of growing plants
JP7004763B2 (en) * 2020-04-07 2022-01-21 積水化学工業株式会社 Method for producing ethanol solution derived from waste, method for producing synthetic product, and method for producing fuel
CN111393681B (en) * 2020-04-17 2021-02-19 华南理工大学 Dynamic covalent cross-linked wood-plastic composite material and preparation method and application thereof
JP2023524653A (en) * 2020-04-22 2023-06-13 ユニバーシティ オブ メリーランド, カレッジ パーク Mouldable and shaped cellulosic structural materials, and systems and methods for their shaping and use
CN111534348B (en) * 2020-05-13 2021-06-04 昌鎏源源新能源科技有限公司 Preparation method of solid-liquid dual-state high-fuel-value biomass fuel
RU2768668C2 (en) * 2020-05-26 2022-03-24 Василий Дмитриевич Мушенко Thermal cracking unit for heavy oil residues
CN111592112A (en) * 2020-05-28 2020-08-28 盐城工学院 Method for remediation and recycling of organic pollution by mudflat plants
MX2023000090A (en) * 2020-07-02 2023-02-23 Univ Louisville Res Found Inc Fiber pretreatment for improved natural fiber - polymer composite feedstock production.
IT202000016651A1 (en) 2020-07-09 2022-01-09 Novamont Spa HYDROLYSIS OF WASTE CELLULOSIC BIOMASS
CN111850070A (en) * 2020-07-28 2020-10-30 暨南大学 Method for pretreating bagasse by using sodium phosphate and hydrogen peroxide
US20230407016A1 (en) * 2020-09-22 2023-12-21 Rensselaer Polytechnic Institute Polysaccharide-including liquid material and its manufacturing method
US20220098685A1 (en) 2020-09-25 2022-03-31 Carbon Technology Holdings, LLC Bio-reduction of metal ores integrated with biomass pyrolysis
EP4225807A2 (en) * 2020-10-12 2023-08-16 GranBio Intellectual Property Holdings, LLC Process for converting lignocellulosic biomass into sugars, biochemicals, biofuels, and biomaterials
CN112226261B (en) * 2020-10-12 2021-06-04 新宁新欣热能科技有限公司 Production method of biological granular fuel
WO2022087579A1 (en) * 2020-10-19 2022-04-28 Cp Energy Services, Inc. Separator system and method
CN112265092B (en) * 2020-10-20 2022-06-17 北京理工大学 Method for simply manufacturing environment-friendly flame-retardant wood and improving mechanical property of environment-friendly flame-retardant wood
CN112626905A (en) * 2020-12-16 2021-04-09 江西中竹生物质科技有限公司 Process for manufacturing wheat straw pulp
CN112961799B (en) * 2021-02-08 2022-10-14 汕头大学 Clostridium and method for preparing biological butanol by using same
CN117015624A (en) 2021-02-18 2023-11-07 卡本科技控股有限责任公司 Carbon negative metallurgical product
US11839225B2 (en) 2021-07-14 2023-12-12 Usarium Inc. Method for manufacturing alternative meat from liquid spent brewers' yeast
CN113549479A (en) * 2021-08-16 2021-10-26 辽宁科技学院 Method for preparing charcoal from waste and old fungus sticks
KR102615764B1 (en) * 2021-09-09 2023-12-20 주식회사 에스피에너지 Manufacturing method of BIO-SRF using waste wood
CN114210692B (en) * 2021-11-05 2022-09-16 新疆冠农果茸股份有限公司 Waste straw pretreatment process in whole material fermentation
DK202170551A1 (en) * 2021-11-11 2023-06-20 Dsm Ip Assets Bv Fermentation system, feed controller, and related methods
CN113862015A (en) * 2021-11-22 2021-12-31 华南农业大学 Method for promoting quality of pyrolysis oil to be improved by seawater electrochemical pretreatment of biomass and application
GB2616246A (en) * 2021-12-21 2023-09-06 Thermo Pressure Tech Limited Thermal-pressure hydrolysis of sustainable biomass for the production of alternative proteins and bio-materials
CN114351487B (en) * 2022-01-18 2023-12-19 浙江恒川新材料有限公司 Wood pulp fiber treatment device for straw body paper production
WO2023170495A1 (en) * 2022-03-08 2023-09-14 Juno Llc System and method for recycling waste material having preshredded step
CN114573995B (en) * 2022-03-12 2022-11-25 昆明理工大学 Preparation method of elastic buffer body taking corn stalks as biological templates
CN115283113B (en) * 2022-03-24 2023-11-10 白银新银鑫工贸有限公司 Feed additive and preparation process thereof
US20230331136A1 (en) * 2022-04-13 2023-10-19 Arbor Fuel Technologies, LLC Biomass Delivery System
JP2023159722A (en) 2022-04-20 2023-11-01 全 信 九 Method for producing glycolic acid and polyglycolic acid
CN115487922B (en) * 2022-07-15 2023-06-02 浙江强村富民竹产业有限公司 Method for preparing diversified products by using plant fibers
CN116283847A (en) * 2023-03-09 2023-06-23 湖南农业大学 Method for simultaneously producing furfural and 5-hydroxymethylfurfural by using metal-rich straw

Citations (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3844890A (en) 1971-09-30 1974-10-29 Rikagaku Kenkyusho Alkaline cellulase and preparation of the same
US4094742A (en) 1977-03-04 1978-06-13 General Electric Company Production of ethanol from cellulose using a thermophilic mixed culture
US4292406A (en) 1979-09-11 1981-09-29 The United States Of America As Represented By The United States Department Of Energy Anaerobic thermophilic culture system
US4435307A (en) 1980-04-30 1984-03-06 Novo Industri A/S Detergent cellulase
EP0458162A1 (en) 1990-05-24 1991-11-27 Kao Corporation Proteinase-resistant cellulase, micro-organism producing the same and process for producing the same
US5370999A (en) 1992-12-17 1994-12-06 Colorado State University Research Foundation Treatment of fibrous lignocellulosic biomass by high shear forces in a turbulent couette flow to make the biomass more susceptible to hydrolysis
US5766764A (en) 1996-06-04 1998-06-16 The Boeing Company Nanoscale amorphous magnetic metals
US5828156A (en) 1996-10-23 1998-10-27 Branson Ultrasonics Corporation Ultrasonic apparatus
US5942649A (en) 1995-06-23 1999-08-24 E. I. Du Pont De Nemours And Company Method for monomer recovery
US5952105A (en) 1997-09-02 1999-09-14 Xyleco, Inc. Poly-coated paper composites
US5973035A (en) 1997-10-31 1999-10-26 Xyleco, Inc. Cellulosic fiber composites
US6383152B1 (en) 1997-01-24 2002-05-07 Siemens Aktiengesellschaft Apparatus for producing shock waves for technical, preferably medical applications
US6448307B1 (en) 1997-09-02 2002-09-10 Xyleco, Inc. Compositions of texturized fibrous materials
US6624539B1 (en) 1997-05-13 2003-09-23 Edge Technologies, Inc. High power ultrasonic transducers
US6737464B1 (en) 2000-05-30 2004-05-18 University Of South Carolina Research Foundation Polymer nanocomposite comprising a matrix polymer and a layered clay material having a low quartz content
US6849680B2 (en) 2001-03-02 2005-02-01 Southern Clay Products, Inc. Preparation of polymer nanocomposites by dispersion destabilization
US6883667B1 (en) 2003-02-12 2005-04-26 Wellman, Inc. Automatic debris separation system
US20060010648A1 (en) 2004-07-16 2006-01-19 Hon Hai Precision Industry Co., Ltd. Hinge assembly
US7074918B2 (en) 1997-09-02 2006-07-11 Xyleco, Inc. Cellulosic and lignocellulosic materials and compositions and composites made therefrom
WO2006102543A2 (en) 2005-03-24 2006-09-28 Xyleco, Inc. Fibrous materials and composites
WO2006110891A2 (en) 2005-04-12 2006-10-19 E. I. Du Pont De Nemours And Company Treatment of biomass to obtain a target chemical
US20070045456A1 (en) 2005-08-24 2007-03-01 Marshall Medoff Fibrous materials and compositions
WO2007071818A1 (en) 2005-12-22 2007-06-28 Roal Oy Treatment of cellulosic material and enzymes useful therein

Family Cites Families (172)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1105705A (en) 1911-07-05 1914-08-04 Near Side Car Company Step and step-operating mechanism.
US1570891A (en) * 1923-03-22 1926-01-26 Heuser Herman Utilizing corncobs
US1750205A (en) 1928-08-20 1930-03-11 Willumsen Oscar Reserve dispensing container
GB572642A (en) * 1941-04-11 1945-10-17 Charles Weizmann Improvements in and relating to the production of aliphatic acids by the fermentation of difficultly fermentable materials
US2567405A (en) 1946-03-13 1951-09-11 Lynch Corp Wrapping machine for sandwiches and the like
US2481263A (en) 1948-01-15 1949-09-06 Us Agriculture Fermentation process
US2610205A (en) 1949-02-02 1952-09-09 Socony Vacuum Oil Co Inc Ester composition
US3093604A (en) 1960-06-30 1963-06-11 Agrashell Inc Composition comprising lignocellulosic extender and oxidized extracted lignin and adhesive solution containing same
US3326788A (en) 1964-01-29 1967-06-20 Union Carbide Corp Cross-linked and epoxidized cellulosic products
US3455853A (en) * 1964-03-09 1969-07-15 Union Oil Co Method for preparing polysaccharide graft copolymers
US3663261A (en) 1967-02-23 1972-05-16 Jorma Kalervo Miettinen Prof Method for preparing plastic impregnated wood by radiation polymerization
US3549510A (en) * 1967-06-12 1970-12-22 Giorgio Corp Di Polymer-treated irradiated bendable sheets of ligno-cellulose and method of making same
US3625845A (en) * 1968-03-08 1971-12-07 Mitsubishi Petrochemical Co Particulate grafted cellulose-polyolefin compositions
SE358891B (en) * 1968-03-08 1973-08-13 Mitsubishi Petrochemical Co
DE1935566A1 (en) * 1968-07-18 1970-01-22 Verbruggen Maria Louisa Preserving natural colour of foodstuffs by treatment - with gases
US3660223A (en) 1968-09-16 1972-05-02 Samuel L Casalina Rigid, flexible and composite solid objects having cellulose containing rice hull particles and radiation induced polymer and method of making same
FR2127677A5 (en) 1971-02-22 1972-10-13 Radiation Dev Co
US3779706A (en) * 1971-10-04 1973-12-18 Energy Sciences Inc Process for bulk sterilization, minimizing chemical and physical damage
US3764475A (en) * 1971-12-22 1973-10-09 Us Army Enzymatic hydrolysis of cellulose to soluble sugars
US3801432A (en) * 1972-02-07 1974-04-02 Radiation Dev Co Ltd Process for subjecting wood chips to irradiation with electrons
GB1446965A (en) 1974-02-14 1976-08-18 Agricultural Vegetable Prod Preparation of food products
CH577940A5 (en) 1974-11-20 1976-07-30 Bbc Brown Boveri & Cie
US4022665A (en) 1974-12-09 1977-05-10 Institute Of Gas Technology Two phase anaerobic digestion
GB1460696A (en) 1975-02-28 1977-01-06 Mo Ex Fabrika Bayanov Im Sovet Method of treating wood
GB1560022A (en) * 1976-10-20 1980-01-30 Gen Electric Biological pre-treatment of lignocellulose to remove lignin
JPS5850799B2 (en) * 1977-02-08 1983-11-12 工業技術院長 How to dispose of organic waste
JPS53125598A (en) 1977-04-08 1978-11-01 Hitachi Ltd Electron ray irradiation device
US4401680A (en) 1979-01-17 1983-08-30 University Of Waterloo Bioconversion of cereal grain straws to protein-enriched product
US5366558A (en) 1979-03-23 1994-11-22 Brink David L Method of treating biomass material
HU180730B (en) 1979-12-29 1983-04-29 Chinoin Gyogyszer Es Vegyeszet Method for producing self-splitting preparation and fodder mixture
JPS5830274B2 (en) 1980-01-14 1983-06-28 日本原子力研究所 New composting method for organic waste
JPS56109886U (en) 1980-01-24 1981-08-25
JPS56124400U (en) 1980-02-21 1981-09-22
US4382847A (en) 1980-03-06 1983-05-10 Arne Akesson Method of manufacturing bonded products of cellulose or cellulose derivatives
JPS6036279B2 (en) 1980-03-07 1985-08-19 キッコーマン株式会社 Manufacturing method of sugar solution
US4368079A (en) 1980-03-18 1983-01-11 New York University Apparatus for chemical conversion of materials and particularly the conversion of cellulose waste to glucose
JPS597439B2 (en) * 1980-07-31 1984-02-18 株式会社日立製作所 Pretreatment method for cellulosic substances
US4304649A (en) 1980-08-25 1981-12-08 The United States Of America As Represented By The Secretary Of Agriculture Solubilization of lignocellulosic materials
US4338399A (en) * 1980-09-15 1982-07-06 Standard Oil Company (Indiana) Process for recovering hydrocarbons from hydrocarbon-containing biomass
US4321328A (en) * 1980-12-05 1982-03-23 Hoge William H Process for making ethanol and fuel product
JPS5915633B2 (en) * 1981-09-30 1984-04-10 新燃料油開発技術研究組合 Enzymatic hydrolysis method for cellulosic materials
JPS5858077B2 (en) * 1981-11-12 1983-12-23 新燃料油開発技術研究組合 Pretreatment method for enzymatic hydrolysis of cellulosic materials
US4398917A (en) * 1982-03-23 1983-08-16 Reilly Charles J Process for the preparation of fuel pellets
US4545607A (en) 1982-09-23 1985-10-08 Leon Yulkowski Door construction
JPS5953840B2 (en) * 1982-10-15 1984-12-27 新燃料油開発技術研究組合 Pretreatment method for enzymatic hydrolysis of cellulose materials
JPS59198987A (en) 1983-04-25 1984-11-10 Osaka Gas Co Ltd Effective utilization of cellulosic material
US4628029A (en) 1983-08-25 1986-12-09 Parsons & Whittemore, Inc. Method for the conversion of a cellulosic substrate to glucose using Microbispora bispora, strain Rutgers P&W
EP0136277A3 (en) 1983-08-31 1986-01-08 Mareck B.V. Gasifier and method for producing combustible gases from biomass material
FR2552125B1 (en) * 1983-09-16 1986-03-21 Interox PROCESS FOR THE TREATMENT OF CELLULOSIC MATERIALS BY OXIDIZING AGENTS
FR2556344A1 (en) 1983-12-12 1985-06-14 British Petroleum Co Process for production of furfural and 5-(hydroxymethyl)furfural and corresponding hydrogenated derivatives
JPS60164494A (en) 1984-02-07 1985-08-27 Res Assoc Petroleum Alternat Dev<Rapad> Method for pretreatment of enzymic hydrolysis of cellulosic wood
JPS60164494U (en) 1984-04-10 1985-10-31 武藤 正志 underwater scooter
FR2567148B1 (en) 1984-07-09 1986-11-14 Comp Generale Electricite PROCESS FOR OBTAINING METHANE BY FERMENTATION OF ALGAE
JPS6178390A (en) * 1984-09-25 1986-04-21 Japan Atom Energy Res Inst Pretreatment for saccharification and fermentation of waste resource of cellulose
JPS6178390U (en) 1984-10-29 1986-05-26
US4584947A (en) 1985-07-01 1986-04-29 Chittick Donald E Fuel gas-producing pyrolysis reactors
JPS6222596A (en) * 1985-07-22 1987-01-30 Res Assoc Petroleum Alternat Dev<Rapad> Method of saccharifying cellulose-containing substance
US4678860A (en) * 1985-10-04 1987-07-07 Arizona Board Of Regents Process of producing liquid hydrocarbon fuels from biomass
JPH0824919B2 (en) 1987-10-09 1996-03-13 サントリー株式会社 Methane fermentation method of distillation bottoms
US4897497A (en) 1988-04-26 1990-01-30 Biofine Incorporated Lignocellulose degradation to furfural and levulinic acid
CS274575B2 (en) 1988-06-13 1991-08-13 Reiner Doc Ing Csc Seifert Method of 2-furaldehyde,cellulose and lignin production from lignocellulosic materials
US5196069A (en) * 1991-07-05 1993-03-23 The United States Of America As Represented By The United States National Aeronautics And Space Administration Apparatus and method for cellulose processing using microwave pretreatment
US5526607A (en) * 1991-08-15 1996-06-18 Net/Tech International Water dispersible delivery system for an agriculturally active chemical
US5395455A (en) * 1992-03-10 1995-03-07 Energy, Mines And Resources - Canada Process for the production of anhydrosugars from lignin and cellulose containing biomass by pyrolysis
JPH05297200A (en) * 1992-04-21 1993-11-12 Sekisui Chem Co Ltd Operating method and device for irradiation bridge by convetor drive
US5865898A (en) * 1992-08-06 1999-02-02 The Texas A&M University System Methods of biomass pretreatment
RU2095415C1 (en) * 1992-12-03 1997-11-10 Татьяна Евгеньевна Огородникова Method of preparing ethanol from cellulose material
IT1262524B (en) * 1993-07-23 1996-07-02 Marco Maltagliati PROCEDURE FOR IMPROVING THE CHARACTERISTICS OF COMBUSTIBLE OILS, IN PARTICULAR OF BIOMASS PYROLYSIS OILS
AU7562294A (en) * 1993-08-13 1995-03-14 Colorado State University Research Foundation Treatment method for lignocellulosic biomass
CA2177984A1 (en) 1993-12-02 1995-06-08 George H. Sparks Processing lignocellulosic agricultural residue
EP0738246B1 (en) 1994-01-03 1997-10-22 ITALTRACO S.r.l. Process for preparing biomass to improve the kinetics of solid-state oxidative biotransformations
US5593779A (en) 1994-06-15 1997-01-14 Kao Corporation Fiber for clothing and production method therefor
JPH08183684A (en) * 1994-12-27 1996-07-16 Satoshi Inoue Production of organic fertilizer
US5932456A (en) * 1995-06-07 1999-08-03 Ingram-Howell, L.L.C. Production of ethanol and other fermentation products from biomass
US5677154A (en) * 1995-06-07 1997-10-14 Ingram-Howell, L.L.C. Production of ethanol from biomass
US5705216A (en) * 1995-08-11 1998-01-06 Tyson; George J. Production of hydrophobic fibers
US5913035A (en) 1995-09-29 1999-06-15 Chrysler Corporation Computer network availability system
JPH09168367A (en) 1995-12-20 1997-06-30 Japan Atom Energy Res Inst Method for producing feed from fibrous cellulosic waste of oil palm
US5753474A (en) 1995-12-26 1998-05-19 Environmental Energy, Inc. Continuous two stage, dual path anaerobic fermentation of butanol and other organic solvents using two different strains of bacteria
CA2244866A1 (en) 1996-01-16 1997-07-24 Cellutech, L.L.C. Pulping ligno-cellulosic material using high frequency radiation
ATE264358T1 (en) * 1997-01-14 2004-04-15 Stockhausen Chem Fab Gmbh INTERMEDIATE PRODUCT FOR THE PRODUCTION OF LIGNIN POLYMERS AND THE USE THEREOF FOR THE PRODUCTION OF REAGENTS FOR THE PRODUCTION OF COMPOSITE MATERIALS FROM VEGETABLE FIBERS, WATERPROOF PAPERS AND PAPERBOARD AND THERMOSETS FROM LIGNIN DERIVATIVES
US6333181B1 (en) 1997-04-07 2001-12-25 University Of Florida Research Foundation, Inc. Ethanol production from lignocellulose
US20030032702A1 (en) * 1997-09-02 2003-02-13 Marshall Medoff Compositions and composites of cellulosic and lignocellulosic materials and resins, and methods of making the same
US20030187102A1 (en) * 1997-09-02 2003-10-02 Marshall Medoff Compositions and composites of cellulosic and lignocellulosic materials and resins, and methods of making the same
DE19756129A1 (en) * 1997-12-17 1999-07-08 Dts Systemoberflaechen Gmbh Making particle board panels of various fibers, especially of waste or recycled materials
JPH11281799A (en) * 1998-03-27 1999-10-15 Ebara Corp Electron beam irradiator
US5952020A (en) * 1998-09-10 1999-09-14 Bio-Feed Ltd. Process of bio-conversion of industrial or agricultural cellulose containing organic wastes into a proteinaceous nutrition product
US6242035B1 (en) * 1998-11-23 2001-06-05 Cp Kelco U.S., Inc. Reduced molecular weight native gellan gum
RU2135510C1 (en) * 1998-12-21 1999-08-27 Общество с ограниченной ответственностью "ПлУГ" Method and installation for processing larch wood
US6446307B2 (en) 1999-02-22 2002-09-10 Electromechanical Research Laboratories, Inc. Manway lid lifter
JP2000279100A (en) 1999-03-31 2000-10-10 San Baiorekkusu:Kk Production of feed
JP2000304900A (en) 1999-04-22 2000-11-02 Natl Food Res Inst Electron beam irradiation device and particle sterilizing method
BR9902606B1 (en) 1999-06-23 2011-04-19 catalytic cellulignin fuel.
SK285761B6 (en) 1999-06-28 2007-07-06 Miroslav Hut�An Process for producing biogas from beet slices, especially from beet sugar production
DE10004241A1 (en) * 2000-02-01 2001-08-02 Werner Falkhof Biodegradable molding composition, comprises cellulose, calcium sulfate, filler, release agent, heat-curable adhesive, binder and colorants
DE60136267D1 (en) 2000-02-17 2008-12-04 Biogasol Ipr Aps METHOD FOR THE TREATMENT OF LIGNIN AND CELLULOSE-CONTAINING SUBSTANCES
ES2166316B1 (en) 2000-02-24 2003-02-16 Ct Investig Energeticas Ciemat PROCEDURE FOR THE PRODUCTION OF ETHANOL FROM LIGNOCELLULOSIC BIOMASS USING A NEW THERMOTOLERING YEAST.
DK200000417A (en) 2000-03-15 2001-09-16 Cowi Radgivende Ingeniorer As Process and plant for decomposition, gasification and / or combustion of moist fuel.
JP4533496B2 (en) 2000-03-15 2010-09-01 三菱重工業株式会社 Fuel production method from biomass
JP2001335390A (en) * 2000-05-22 2001-12-04 Kuniharu Kensetsu Kk Method of manufacturing organic manure
FI20001612A (en) * 2000-07-05 2002-02-13 Dynea Chemicals Oy Process for making fibreboard
DE10043662A1 (en) * 2000-08-30 2001-02-22 Saechsisches Inst Fuer Angewan Production of lignocellulosic fiber products, e.g. fiberboard, comprises treating the fibers with hydrolytic enzymes during or after disintegration to improve adhesion
US6454944B1 (en) * 2000-11-08 2002-09-24 Larry J. Raven Process and apparatus for conversion of biodegradable organic materials into product gas
JP2002210434A (en) * 2000-11-17 2002-07-30 Mitsubishi Heavy Ind Ltd Decomposition processing method for halogenized organic compound and apparatus therefor
US20050020829A1 (en) * 2000-12-04 2005-01-27 Shigetaka Yamamoto Treatment method for wooden material
JP2002180064A (en) 2000-12-14 2002-06-26 Takeji Motai Artificial charcoal and method and producing the same
US6908995B2 (en) * 2001-01-05 2005-06-21 David H. Blount Production of carbohydrates, alcohol and resins from biomass
JP2002254054A (en) * 2001-02-28 2002-09-10 Eemu:Kk Method for disposing of garbage and garbage disposer
US6506712B2 (en) * 2001-05-21 2003-01-14 React, Llc Method of manufacturing a multifunctional additive and using the same
US20040138445A1 (en) 2001-07-10 2004-07-15 Thorre Doug Van Process for obtaining bio-functional fractions from biomass
JP3801499B2 (en) * 2001-07-19 2006-07-26 三菱重工業株式会社 Method and apparatus for treating organic waste
US6835560B2 (en) 2001-10-18 2004-12-28 Clemson University Process for ozonating and converting organic materials into useful products
CA2466505A1 (en) 2001-11-09 2003-05-15 Biopulping International, Inc. Microwave pre-treatment of logs for use in making paper and other wood products
JP2003215300A (en) * 2002-01-28 2003-07-30 Mitsubishi Heavy Ind Ltd Electron beam irradiator
US7396974B2 (en) * 2002-02-08 2008-07-08 University Of Maine Oxidation using a non-enzymatic free radical system mediated by redox cycling chelators
JP2003279699A (en) * 2002-03-22 2003-10-02 Mitsubishi Heavy Ind Ltd Electron beam irradiation processing device
JP2003305437A (en) * 2002-04-17 2003-10-28 Toru Ueda Method for treating solid organic matter combining photoirradiation and slaked lime addition and garbage disposal apparatus using this method
US6953873B2 (en) 2002-05-10 2005-10-11 Wisconsin Alumni Research Foundation Low-temperature hydrocarbon production from oxygenated hydrocarbons
EP1382435A1 (en) * 2002-07-12 2004-01-21 Canon Kabushiki Kaisha Molded product for cushioning material, and production process and recovery thereof
US20060088630A1 (en) * 2002-07-22 2006-04-27 Fox Eugene J Process for sonicating plant seeds
JP2004050143A (en) * 2002-07-24 2004-02-19 Mitsubishi Kakoki Kaisha Ltd Treating method of organic waste
JP4184021B2 (en) * 2002-09-30 2008-11-19 月島機械株式会社 Method for producing alcohol
JP2004187650A (en) * 2002-10-17 2004-07-08 Tsukishima Kikai Co Ltd Method for producing alcohol or organic acid from waste construction material
US6808600B2 (en) * 2002-11-08 2004-10-26 Kimberly-Clark Worldwide, Inc. Method for enhancing the softness of paper-based products
JP4025629B2 (en) * 2002-11-20 2007-12-26 株式会社神戸製鋼所 Organic waste treatment methods
JP2004261144A (en) 2003-03-04 2004-09-24 Japan Science & Technology Agency Recombinant microorganism, anaerobic digestion method for organic waste
DE60320041T2 (en) * 2003-03-12 2009-04-16 Sekisui Chemical Co., Ltd. DEVICE FOR ALIGNING AND LAMINATING WOODEN PAINTS AND METHOD FOR MANUFACTURING WOOD COMPOSITE MATERIAL
ITBZ20030024A1 (en) 2003-04-30 2004-11-01 Ziegelei Gasser Gmbh Srl PROCEDURE AND PLANT FOR THE ANAEROBIC FERMENTATION OF BIOMASSES WITH PRODUCTION OF BIOGAS.
DE10327954C5 (en) 2003-06-20 2008-06-26 Wilkening, Carl Ludwig, Dr. Improved processes for the production of ethanol and methane from cereals
US20050017502A1 (en) 2003-07-21 2005-01-27 Chariker Sean Keith Foldable data-card assembly
US20050026262A1 (en) * 2003-07-30 2005-02-03 Sonoenergy, Llc Sonication-enhanced digestion process
WO2005021742A2 (en) * 2003-08-29 2005-03-10 Ultraforce Technology Llc Alcohol production using sonication
JP2005081317A (en) * 2003-09-11 2005-03-31 Masahiro Yoshimoto Ozone reactor
JP2005087940A (en) 2003-09-19 2005-04-07 Masahiro Yoshimoto Integrated system for utilization of resource
US7504245B2 (en) * 2003-10-03 2009-03-17 Fcstone Carbon, Llc Biomass conversion to alcohol using ultrasonic energy
ITTP20030002A1 (en) * 2003-10-09 2005-04-10 Giovanni Maurizio Di OXIDORIDUTION PROCESS TO RECYCLE ANY REJECTION FRACTION: SLUDGE, INDUSTRIAL WASTE, AGRI-FOOD, SLAUGHTER, FISH, ETC. IN STERILE BIOSTABILIZED AND / OR THERMOACOUSTIC EXPANDED POLYXAN INSULATION, IN AN INNOVATIVE MOBILE OR FIXED SYSTEM WITH
JP4405239B2 (en) * 2003-11-11 2010-01-27 株式会社Ihi Organic waste treatment apparatus and method
JP2005172534A (en) * 2003-12-10 2005-06-30 Nhv Corporation Electron beam irradiation device
WO2005063946A1 (en) * 2003-12-31 2005-07-14 Iwi (Holdings) Limited Method and apparatus for processing mixed organic waste
US7354743B2 (en) 2004-01-16 2008-04-08 Novozymes, Inc. Methods for degrading lignocellulosic materials
KR100569738B1 (en) 2004-04-02 2006-04-11 윤현희 Method of Lactic Acid Production Using Fibrous Biomass
CN101018866A (en) * 2004-05-03 2007-08-15 Ut巴特勒有限公司 A method to produce succinic acid from raw hydrolysates
US20070029264A1 (en) 2004-06-15 2007-02-08 Bowe Michael J Processing biological waste materials to provide energy
ES2246708B1 (en) 2004-06-18 2007-04-01 Diseño De Sistemas En Silicio, S.A. PROCEDURE FOR OBTAINING SPECTRAL HOLES IN THE TRANSMISSION OF SIGNS BY THE ELECTRICAL NETWORK.
ZA200404951B (en) 2004-06-23 2005-04-26 Du Toit System and method for handling calcium compound slurries.
CA2579024A1 (en) 2004-07-09 2006-02-16 Earnest Stuart Effect of radiation on cellulase enzymes
JP2006042719A (en) * 2004-08-06 2006-02-16 Toyota Central Res & Dev Lab Inc Microorganism producing organic acid, and its use
US8414822B2 (en) 2004-09-24 2013-04-09 Ion Beam Applications, S.A. Processes for chemically affecting reactive materials with X-rays
JP2006095439A (en) * 2004-09-29 2006-04-13 Yoshinori Hayashi Method for treating organic waste
RU2265663C1 (en) * 2004-11-25 2005-12-10 Государственное образовательное учреждение высшего профессионального образования "Московский государственный университет пищевых производств" Министерства образования Российской Федерации Method for producing ethyl alcohol
BRPI0516665B8 (en) 2004-11-29 2022-08-09 Elsam Eng A/S PROCESSES FOR LIQUEFATION OF BIOMASSES CONTAINING POLYSACCHARIDE
BRPI0515786A2 (en) * 2004-12-17 2011-10-11 Iogen Energy Corp upflow settling reactor for enzymatic cellulose hydrolysis
US20070125369A1 (en) 2005-02-07 2007-06-07 Olson Edwin S Process for converting anhydrosugars to glucose and other fermentable sugars
BRPI0500534A (en) 2005-02-15 2006-10-10 Oxiteno Sa Ind E Comercio acid hydrolysis process of cellulosic and lignocellulosic materials, digestion vessel and hydrolysis reactor
JP2006255691A (en) * 2005-02-17 2006-09-28 Sumitomo Chemical Co Ltd Environment cleaning material and method using the same
JP2006255676A (en) 2005-03-18 2006-09-28 Kri Inc Method for separating lignin substance
US7902407B2 (en) * 2005-03-30 2011-03-08 Sabic Innovative Plastics Ip B.V. Method for preparation of salts of hydroxy-substituted aromatic compounds
JP2006281024A (en) * 2005-03-31 2006-10-19 Tsukishima Kikai Co Ltd Adsorbent, its manufacturing method and method for producing alcohol or organic acid
US7566383B2 (en) 2005-06-17 2009-07-28 Purdue Research Foundation Heat recovery from a biomass heat source
DE102005032395A1 (en) 2005-07-12 2007-01-25 Mahle International Gmbh Filter medium for technical applications and method of its production
DK1910448T3 (en) * 2005-07-19 2017-01-02 Inbicon As METHOD AND APPARATUS FOR CONVERSION OF CELLULOS MATERIAL TO ETHANOL
WO2007089290A2 (en) 2005-09-30 2007-08-09 Novozymes, Inc. Methods for enhancing the degradation or conversion of cellulosic material
PL1954798T3 (en) 2005-09-30 2010-08-31 Renescience As Non-pressurised pre-treatment, enzymatic hydrolysis and fermentation of waste fractions
CN100516228C (en) * 2005-12-29 2009-07-22 陕西科技大学 Method for preprocessing biomass
AU2007210012B2 (en) * 2006-01-27 2012-04-05 University Of Massachussetts Systems and methods for producing biofuels and related materials
DE102006007458B4 (en) 2006-02-17 2010-07-08 Native Power Solutions Gmbh & Co. Kg Method and apparatus for gasifying carbonaceous material and apparatus for generating electrical energy
WO2007100897A2 (en) * 2006-02-27 2007-09-07 Edenspace System Corporation Energy crops for improved biofuel feedstocks
EP2049247A2 (en) * 2006-07-17 2009-04-22 BIOeCON International Holding N.V. Electro-magnetic treatment of a modified biomass
AP2724A (en) 2006-07-21 2013-08-31 Xyleco Inc Conversion systems for biomass
CA2823361C (en) 2006-10-26 2014-09-16 Xyleco, Inc. Methods of processing biomass comprising electron-beam radiation
KR100873700B1 (en) 2007-06-25 2008-12-12 사단법인 한국가속기 및 플라즈마 연구협회 Method of producing bio-fuel using electron beam
US7846295B1 (en) 2008-04-30 2010-12-07 Xyleco, Inc. Cellulosic and lignocellulosic structural materials and methods and systems for manufacturing such materials

Patent Citations (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3844890A (en) 1971-09-30 1974-10-29 Rikagaku Kenkyusho Alkaline cellulase and preparation of the same
US4094742A (en) 1977-03-04 1978-06-13 General Electric Company Production of ethanol from cellulose using a thermophilic mixed culture
US4292406A (en) 1979-09-11 1981-09-29 The United States Of America As Represented By The United States Department Of Energy Anaerobic thermophilic culture system
US4435307A (en) 1980-04-30 1984-03-06 Novo Industri A/S Detergent cellulase
EP0458162A1 (en) 1990-05-24 1991-11-27 Kao Corporation Proteinase-resistant cellulase, micro-organism producing the same and process for producing the same
US5370999A (en) 1992-12-17 1994-12-06 Colorado State University Research Foundation Treatment of fibrous lignocellulosic biomass by high shear forces in a turbulent couette flow to make the biomass more susceptible to hydrolysis
US5942649A (en) 1995-06-23 1999-08-24 E. I. Du Pont De Nemours And Company Method for monomer recovery
US5766764A (en) 1996-06-04 1998-06-16 The Boeing Company Nanoscale amorphous magnetic metals
US5828156A (en) 1996-10-23 1998-10-27 Branson Ultrasonics Corporation Ultrasonic apparatus
US6383152B1 (en) 1997-01-24 2002-05-07 Siemens Aktiengesellschaft Apparatus for producing shock waves for technical, preferably medical applications
US6624539B1 (en) 1997-05-13 2003-09-23 Edge Technologies, Inc. High power ultrasonic transducers
US5952105A (en) 1997-09-02 1999-09-14 Xyleco, Inc. Poly-coated paper composites
US7074918B2 (en) 1997-09-02 2006-07-11 Xyleco, Inc. Cellulosic and lignocellulosic materials and compositions and composites made therefrom
US6448307B1 (en) 1997-09-02 2002-09-10 Xyleco, Inc. Compositions of texturized fibrous materials
US6258876B1 (en) 1997-10-31 2001-07-10 Xyleco, Inc. Cellulosic fiber composites
US6207729B1 (en) 1997-10-31 2001-03-27 Xyleco, Inc. Texturized cellulosic and lignocellulosic materials and compositions and composites made therefrom
US5973035A (en) 1997-10-31 1999-10-26 Xyleco, Inc. Cellulosic fiber composites
US6737464B1 (en) 2000-05-30 2004-05-18 University Of South Carolina Research Foundation Polymer nanocomposite comprising a matrix polymer and a layered clay material having a low quartz content
US6849680B2 (en) 2001-03-02 2005-02-01 Southern Clay Products, Inc. Preparation of polymer nanocomposites by dispersion destabilization
US6883667B1 (en) 2003-02-12 2005-04-26 Wellman, Inc. Automatic debris separation system
US20060010648A1 (en) 2004-07-16 2006-01-19 Hon Hai Precision Industry Co., Ltd. Hinge assembly
WO2006102543A2 (en) 2005-03-24 2006-09-28 Xyleco, Inc. Fibrous materials and composites
WO2006110891A2 (en) 2005-04-12 2006-10-19 E. I. Du Pont De Nemours And Company Treatment of biomass to obtain a target chemical
US20070045456A1 (en) 2005-08-24 2007-03-01 Marshall Medoff Fibrous materials and compositions
WO2007071818A1 (en) 2005-12-22 2007-06-28 Roal Oy Treatment of cellulosic material and enzymes useful therein

Non-Patent Citations (31)

* Cited by examiner, † Cited by third party
Title
AHRING ET AL., ARCH. MICROBIOL, vol. 168, 1997, pages 114 - 119
AVIVI ET AL., J. AMER. CHEM. SOC., vol. 121, 1999, pages 4196
AVIVI ET AL., J. AMER. CHEM. SOC., vol. 122, 2000, pages 4331
BAILEY, J.E., OLLIS, D.F.: "Biochemical EngineeringFundamentals", 1986, MCGRAW-HILL BOOK COMPANY
BARBER ET AL., NATURE, vol. 352, 1991, pages 414
BENNETT, J.W. AND LASURE, L.: "More Gene Manipulations in Fungi", 1991, ACADEMIC PRESS
BOUCHARD ET AL., CELLULOSE, vol. 13, 2006, pages 601 - 610
DIPARDO, JOURNAL OF OUTLOOK FOR BIOMASS ETHANOL PRODUCTION AND DEMAND (EIA FORECASTS, 2002
GHOSE, PURE AND APPL. CHEM., vol. 59, 1987, pages 257 - 268
GREER, BIOCYCLE, April 2005 (2005-04-01), pages 61 - 65
HILLER ET AL., PHYS. REV. LETT., vol. 69, 1992, pages 1182
HOPE, DEAN, BIOTECH J., vol. 144, 1974, pages 403
LANDAU ET AL., J. OF CATALYSIS, vol. 201, 2001, pages 22
LESCHINE ET AL., INTERNATIONAL JOURNAL OF SYSTEMATIC AND EVOLUTIONARY MICROBIOLOGY, vol. 52, 2002, pages 1155 - 1160
LESCHINE, INTERNATIONAL JOURNAL OF SYSTEMATIC AND EVOLUTIONARY MICROBIOLOGY, vol. 52, 2002, pages 1155 - 1160
LYND, MICROBIOLOGY AND MOLECULAR BIOLOGY REVIEWS, vol. 66, no. 3, 2002, pages 506 - 577
MARTIN, ENZYME MICROBES TECHNOLOGY, vol. 31, 2002, pages 274
MASON: "Chemistry with Ultrasound", 1990, ELSEVIER
NIKITENKO ET AL., ANGEW. CHEM. INTER. ED., December 2001 (2001-12-01)
PERKAS ET AL., CHEM. COMM., 2001, pages 988
PRICE: "Current Trends in Sonochemistry", 1992, ROYAL SOCIETY OF CHEMISTRY
SHAFI ET AL., J. PHYS. CHEM B, vol. 103, 1999, pages 3358
SHEEHAN, BIOTECHNOLOGY PROGRESS, vol. 15, 1999, pages 8179
SONNE-HANSEN ET AL., APPLIED MICROBIOLOGY AND BIOTECHNOLOGY, vol. 38, 1993, pages 537 - 541
SUSLICK ET AL., ANN. REV. MATER. SCI., vol. 29, 1999, pages 295
SUSLICK ET AL., J. AM. CHEM. SOC., vol. 108, 1986, pages 5641
SUSLICK ET AL., NATURE, vol. 353, 1991, pages 414
SUSLICK ET AL., NATURE, vol. 434, pages 52 - 55
SUSLICK: "Ultrasound: its Chemical, Physical and Biological Effects", 1988, VCH
TANG ET AL., CHEM. COMM., 2000, pages 2119
WANG ET AL., ADVANCED MATER., vol. 12, 2000, pages 1137

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